CN110960956A - Be applicable to phase transition absorbent and absorb CO in flue gas2Method and system - Google Patents
Be applicable to phase transition absorbent and absorb CO in flue gas2Method and system Download PDFInfo
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- CN110960956A CN110960956A CN201911214630.8A CN201911214630A CN110960956A CN 110960956 A CN110960956 A CN 110960956A CN 201911214630 A CN201911214630 A CN 201911214630A CN 110960956 A CN110960956 A CN 110960956A
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- 239000002250 absorbent Substances 0.000 title claims abstract description 135
- 230000002745 absorbent Effects 0.000 title claims abstract description 119
- 230000007704 transition Effects 0.000 title claims description 5
- 238000010521 absorption reaction Methods 0.000 claims abstract description 177
- 239000012071 phase Substances 0.000 claims abstract description 115
- 230000008859 change Effects 0.000 claims abstract description 75
- 239000003546 flue gas Substances 0.000 claims abstract description 66
- 239000007791 liquid phase Substances 0.000 claims abstract description 60
- 238000005191 phase separation Methods 0.000 claims abstract description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 230000008569 process Effects 0.000 claims abstract description 7
- 230000009102 absorption Effects 0.000 claims description 162
- 238000003795 desorption Methods 0.000 claims description 19
- 238000004064 recycling Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000009103 reabsorption Effects 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 13
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 125000004122 cyclic group Chemical group 0.000 abstract description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 51
- 238000005070 sampling Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 241000282414 Homo sapiens Species 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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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
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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
- B01D53/1425—Regeneration of liquid absorbents
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- 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
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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
- 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
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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
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a phase change absorbent for absorbing CO in flue gas2The method is suitable for absorbing CO in the flue gas by the phase change absorbent2The technology adopts a phase-change absorbent to absorb CO in the flue gas2Absorbing CO2The phase separation is carried out on the solution, and the CO after the phase separation2The rich liquid is continuously used for treating CO in the flue gas2Absorbing CO in the flue gas by using a phase change absorbent2And with CO2Rich liquid phase absorbing CO in flue gas2The process is carried out in different absorption towers to absorb CO in the flue gas again2CO of2Desorbing the rich solution, and separating the desorbed solution from the phase-separated CO2The lean liquid phase is mixed and then is continuously used for treating CO in the flue gas2Absorption is carried out. The invention can effectively improve CO in the flue gas2The absorption efficiency of the phase change absorbent and CO is realized2The mass transfer efficiency in the absorption tower is optimized, the cyclic utilization of the phase-change absorbent can be realized, and the mass transfer efficiency is reducedLow CO2And (4) desorbing energy consumption of the pregnant solution.
Description
Technical Field
The invention relates to a method for absorbing CO in flue gas2Especially to a method and a system suitable for absorbing CO in flue gas by a phase change absorbent2The method is suitable for absorbing CO in the flue gas by the phase change absorbent2The absorption system of (1).
Background
In recent years, CO has become a cause of2The 'greenhouse effect' caused by the main greenhouse gas poses serious threat to the living environment of human beings, and at present, CO2Emission reduction has become a common human consensus. Carbon Capture and Storage (CCS) technology is a viable approach to control and curtail global Carbon dioxide emissions. Among CCS technologies, the chemical absorption method is the most mature technology due to its large absorption capacity, and is currently the most widely used CO2However, this technique always has a problem of excessively high regeneration energy consumption.
Researchers provided efficient and low-energy-consumption phase change absorbents in CO absorption in the last decade2The former is homogeneous and absorbs CO2After-generation of liquid-liquid phase separation and absorption of CO2Is concentrated in the lower liquid phase, so that only the lower liquid phase needs to be sent into a desorption device, and the lower liquid phase is greatly reduced to enter the desorption deviceThe liquid quantity of the device can be absorbed, the evaporation latent heat and the heating sensible heat energy consumption can be effectively reduced, and the low energy consumption CO can be realized2Trapping, and is expected to be applied to CO in flue gas of large-scale coal-fired power plants2And (4) trapping.
Unlike conventional absorbents, phase change absorbents are used to absorb CO2Phase separation occurs in the process, but at the moment, due to the influence of phase balance, the lower liquid phase after phase separation still does not reach the saturated absorption capacity and still has certain CO2Absorption capacity, high viscosity of lower liquid phase after phase separation, resulting in absorption agent and CO2The mass transfer coefficient is reduced, and the absorption rate is obviously reduced, so that the size of the absorption tower needs to be greatly increased during design, and the equipment investment is increased. On the other hand, in a predetermined absorption tower, the phase change absorbent undergoes phase separation, and the viscosity increases, and the absorption rate decreases, resulting in a large decrease in the throughput and a rapid increase in the running cost. Because the viscosity of the phase change absorbent is changed sharply before and after phase separation, and the mass transfer coefficient in the absorption tower is changed suddenly, different design requirements are required to be provided for the absorption tower before and after phase separation of the absorbent, so that the optimization of the mass transfer efficiency in the same absorption tower is difficult to realize.
Method for achieving CO compromise by adopting high-temperature absorption tower and low-temperature absorption tower2The technology of two key parameters of absorption capacity and viscosity of absorbent is provided, and the upper liquid phase after phase separation returns to the low-temperature absorption tower to continuously absorb CO2The viscosity of the absorbent is reduced by arranging a high-temperature tower, but the technology needs to arrange a heat exchanger between the two towers, and the investment cost is additionally increased. More importantly, the technology separates an upper liquid phase from a lower liquid phase when the absorbent is subjected to phase separation, so that the upper liquid continuously absorbs CO2. Of the phase change absorbents reported to date, one major class of phase change absorbents is in absorbing CO2After phase separation, the upper liquid phase has almost no absorption capacity any more, so the process flow of the technology only can further reduce the viscosity of the absorbent before absorption for the phase-change absorbent, but does not play a role in the lower liquid phase which is phase-separated and has further absorption capacity, namely, the purpose of improving the absorption capacity of the phase-change absorbent cannot be achieved. The art has proposed the use of phase change absorbersCapturing CO2However, the method has no practical effect on the main phase change absorbent, and does not really solve the problem of mass transfer efficiency reduction caused by the sharp increase of viscosity.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides a phase change absorbent for absorbing CO in smoke2The method is suitable for absorbing CO in the flue gas by the phase change absorbent2The absorption system can effectively improve CO in the flue gas2The absorption efficiency of the phase change absorbent and CO is realized2Optimizing the mass transfer efficiency in the absorption tower.
The technical scheme for realizing the aim of the invention is as follows: be applicable to phase transition absorbent and absorb CO in flue gas2The method adopts the original phase-change absorbent (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 treat CO in the flue gas2Absorbing CO2The phase separation is carried out on the solution, and the CO after the phase separation2The rich liquid is continuously used for treating CO in the flue gas2Absorbing, namely absorbing CO in the flue gas by adopting an original phase change absorbent2And using CO after phase separation2Rich liquid phase absorbing CO in flue gas2The process of (a) is carried out in different absorption columns.
Further, to absorb CO again2After CO2Desorbing the rich solution, and separating the desorbed solution from the phase-separated CO2The lean liquid phase is added after being mixed or used as an original phase change absorbent for recycling.
Further, the phase change absorbent is an amine-organic solvent-water system phase change absorbent.
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.
Further, the separated CO2The viscosity of the rich liquid phase is in the range of 10-200 mPas.
Generally, the operating pressure of the different absorption towers is normal pressure, and the working temperature in the different absorption towers is 30-60 ℃.
Be applicable to phase transition absorbent and absorb CO in flue gas2The absorption system comprises a first absorption tower, a second absorption tower and a phase splitter, 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 splitter, a rich liquid phase outlet of the phase splitter is communicated with the absorbent inlet of the second absorption tower, the first absorption tower is used for absorption reaction of an original phase-change absorbent, and the second absorption tower is used for absorption reaction of the phase-split CO2Absorption reaction of rich liquid phase, and phase separator for absorbing CO2Phase separation of the latter original phase change absorbent.
Further, the system also includes CO2A solution outlet of the second absorption tower is communicated with an inlet of the desorption device, a liquid phase outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, a lean liquid phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower, and the desorption device is used for absorbing CO again2After CO2And (4) desorbing the rich solution.
Furthermore, a first conveying pump is installed on an absorbent conveying pipeline communicated with the absorbent inlet of the first absorption tower, and a second conveying pump is installed on a conveying pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower.
The invention has the beneficial effects that:
1. the invention respectively utilizes the phase change absorbent and the phase change absorbent to absorb CO through different absorption towers2After CO2Rich solution relative to CO in flue gas2Compared with the traditional technology adopting a single absorption tower, the absorption can realize the phase change absorbent and CO2Optimization of mass transfer efficiency in the absorption tower and avoidance of phase change absorptionThe mass transfer coefficient in the absorption tower is reduced suddenly due to the rapid change of the viscosity of the absorbent before and after phase separation, and the CO content of the phase-change absorbent can be effectively improved2The absorption efficiency of (2) and (3) can also be realized2Rich liquid relative to CO2The 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 control of CO2Desorbing the solution of the rich solution and CO2And the lean liquid phase is recycled, so that the recycling of the phase change absorbent is realized, the utilization efficiency of the phase change absorbent is improved, and the production cost is reduced.
3. The invention only mixes CO2Compared with the prior art, the method can effectively reduce the amount of the solution entering the desorption device and reduce the desorption energy consumption.
Drawings
FIG. 1 shows that the phase change absorbent of the present invention is suitable for absorbing CO in flue gas2A schematic structural view of one embodiment of the absorbent system of (a);
FIG. 2 shows that the phase change absorbent of the present invention is suitable for absorbing CO in flue gas2Schematic structural representation of another embodiment of the absorbent system of (1).
Detailed Description
The invention discloses a phase change absorbent for absorbing CO in flue gas2The method adopts the phase-change absorbent (which can be called as the original phase-change absorbent) to treat CO in the flue gas2Absorbing CO2The phase separation is carried out on the solution, and the CO after the phase separation2The rich liquid is continuously used for treating CO in the flue gas2Absorbing CO in the flue gas by using a phase change absorbent2And with CO2Rich liquid phase absorbing CO in flue gas2The process of (a) is carried out in different absorption columns. Further, the CO in the flue gas is absorbed again2CO of2Desorbing the rich solution, and separating the desorbed solution from the phase-separated CO2Mixing the barren solution phase and recovering the homogeneous phase, and then continuously using the barren solution phase for CO in the flue gas2Absorption is carried out.
In the usual case, adoptThe method is realized by two absorption towers which are respectively 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 an air outlet at the top end of the second absorption tower, so that flue gas entering the second absorption tower can be sent into the first absorption tower for CO (carbon monoxide) treatment2The working process of the secondary absorption is as follows: containing CO2The 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 absorbs CO in the first absorption tower firstly2(phase Change absorbent with CO2Mass transfer occurs), the phase change absorbent absorbs CO2The phase separation of the solution is carried out at the bottom of the first absorption tower, and the solution is preferably separated into CO by a phase separator2Rich liquid phase and CO2Lean liquid phase, high viscosity CO2Sending the rich liquid phase into the second absorption tower from the upper part of the second absorption tower, and carrying out countercurrent contact with the high-concentration flue gas entering the second absorption tower from the bottom end of the second absorption tower to absorb CO in the flue gas again2CO of2The rich solution flows out from the lower part of the second absorption tower and is sent into a desorption device, and the solution after desorption and the CO after phase separation2The lean solution is mixed and recovered to be homogeneous, and then is sent into the first absorption tower from the upper part of the first absorption tower for cyclic utilization, and is continuously used for CO in the flue gas2Absorption is carried out.
The invention respectively utilizes the phase change absorbent and the phase change absorbent to absorb CO through different absorption towers2After CO2Rich solution relative to CO in flue gas2Compared with the traditional technology adopting a single absorption tower, the absorption can realize the phase change absorbent and CO2The mass transfer efficiency in the absorption tower is optimized, the condition that the mass transfer coefficient in the absorption tower is suddenly reduced due to the rapid change of the viscosity of the phase-change absorbent before and after phase splitting is avoided, and the effect of the phase-change absorbent on CO can be effectively improved2The absorption efficiency of (2) and (3) can also be realized2Rich liquid relative to CO2The absorption capacity can be reused, the size of the absorption tower does not need to be changed, and the equipment is reducedInvestment and operating costs. The invention can realize the control of CO2Desorbing the solution of the rich solution and CO2And the lean liquid phase is recycled, so that the recycling of the phase change absorbent is realized, the utilization efficiency of the phase change absorbent is improved, and the production cost is reduced. The invention only mixes CO2Compared with the prior art, the method can effectively reduce the amount of the solution entering the desorption device and reduce the desorption energy consumption.
The phase change absorbent is an absorbent of an amine-organic solvent-water system, and the phase change absorbent can be ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water.
The viscosity of the phase change absorbent is preferably in the range of 2 to 10 mPas, such as 2 mPas, 5 mPas, 8 mPas or 10 mPas. CO after phase separation2The viscosity of the rich liquid phase is preferably in the range of 10 to 200 mPas, such as 10 mPas, 100 mPas, 150 mPas or 200 mPas.
Generally, the operating pressure of the different absorption towers is normal pressure, and the working temperature in the different absorption towers is 30-60 ℃, such as 30 ℃, 40 ℃, 50 ℃ or 60 ℃.
Referring to fig. 1 and fig. 2, the invention also discloses a method for absorbing CO in flue gas by using the phase change absorbent2The absorption system 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 exhaust port 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 contains CO2The flue gas enters the system from the gas inlet at the bottom of the second absorption tower, the phase-change absorbent enters the first absorption tower from the absorbent inlet at the upper part of the first absorption tower, the gas inlet of the first absorption tower is communicated with the gas outlet of the second absorption tower, so that the flue gas in the second absorption tower can enter the first absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase separator, and the phase separator is used for absorbing CO by the phase-change absorbent in the first absorption tower2The solution after the phase separation is carried out, and a rich liquid phase outlet of the phase separator is communicated with the second absorption tankAn absorbent inlet of the tower for separating the phase-separated CO2The rich liquid phase is sent to the second absorption tower to lead CO to be generated2The rich liquid phase is in countercurrent contact with the high-concentration flue gas entering from the tower bottom of the second absorption tower, and the CO in the flue gas is continuously absorbed2Generally, the lower liquid phase after the phase separation of the phase separator is a rich liquid phase.
Further, the system also includes CO2A solution outlet of the second absorption tower is communicated with an inlet of the desorption device and is used for absorbing CO in the flue gas again2CO of2Rich solution is sent into the desorption device for desorption, an outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, a lean solution phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower, and the lean solution phase outlet is used for separating the solution after desorption and the CO after phase separation2The lean liquid phase is sent into the first absorption tower for cyclic utilization and is continuously used for CO in the flue gas2Absorption is carried out, and in general, the upper liquid phase after the phase separation of the phase separator is a lean liquid phase. Solution after convenient resolution and CO after phase separation2And mixing the lean liquid phase and the lean liquid phase, namely feeding the lean liquid phase and the lean liquid phase into a mixing device to be mixed and return to a homogeneous phase, and then feeding the lean liquid phase and the homogeneous phase into the first absorption tower from an absorbent inlet of the first absorption tower.
Usually, a first delivery pump 4 is installed on an absorbent delivery pipeline communicated with the absorbent inlet of the first absorption tower to facilitate delivery of the phase-change absorbent, and a second delivery pump 5 is installed on a delivery pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower to facilitate delivery of the CO2And (3) conveying the rich liquid phase, and installing a suitable conveying pump on other conveying pipelines to facilitate the conveying of the substances in the pipelines.
Experimental example 1: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, and the lower liquid phase is pumped into the top of a second absorption tower by a second delivery pump atAbsorbing CO in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich solution, and measuring the viscosity to be 29 mPas, CO2The loading was 2.2mol/kg and the required absorption time was 4h in total.
Experimental example 2: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 2.2m3The flow rate of the phase-change absorbent B (with the initial viscosity of 5.2 mPa · s) is fed into the top of the first absorption tower through a first transfer pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich solution, and measuring the viscosity to be 77 mPas, CO2The loading was 2.8 mol/kg and the required absorption time was a total of 2.5 h.
Experimental example 3: 30 ℃ flue gas (CO)2Concentration 50vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich solution, and determining that the viscosity is 49 mPa & s, CO2The loading was 2.4mol/kg and the required absorption time was 4h in total.
Experimental example 4: 40 ℃ flue gas (pure CO)2) At 2.2m3The flow rate of the phase-change absorbent B (with the initial viscosity of 5.2 mPa · s) is fed into the top of the first absorption tower through a first transfer pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich phase, and determining the viscosity to be 127 mPa & s, CO2The loading was 3.5mol/kg and the required absorption time was a total of 2.5 h.
It can be seen from the experimental examplesThe technology of the invention is completely suitable for CO in the flue gas2Absorption is carried out.
Comparative example 1 (conventional technical principle): 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase change absorbent A is fed from the bottom of the second absorption tower, the phase change absorbent A (with the initial viscosity of 7.7 mPa · s) is sent to the top of the first absorption tower by a first delivery pump to circularly absorb CO2The flow rate is 20L/h, and the phase change absorbent absorbs CO after absorbing for 4h2Standing the solution for layering, taking off the liquid phase, and measuring CO2The loading was 1.4 mol/kg.
As can be seen from the comparison of Experimental example 1 with comparative example 1, CO is absorbed in the same period of time2Experimental example 1 can make CO2CO in rich solution2The load is increased from 1.4 mol/kg to 2.2mol/kg, and compared with the prior art, the technology of the invention has the advantage that CO is added2The absorption efficiency of (2) is greatly improved.
Comparative example 2: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the loading capacity of the upper liquid phase is measured by sampling and is 0.2 mol/kg, the upper liquid phase is pumped into the top of a first absorption tower for cyclic absorption for 5 hours, and CO is measured by sampling2The load was still 0.2 mol/kg.
Recycle of front and rear middle CO through upper liquid phase after phase separation in comparative example 22Comparison of loading capacity shows that the technology is suitable for the phase change absorbent (absorbing CO) of an amine-organic solvent-water system2The upper liquid phase of the split-phase solution does not have CO any more2Absorbent for absorbing capacity) of the flue gas2Absorption of (2).
Claims (10)
1. Be applicable to phase transition absorbent and absorb CO in flue gas2The method is characterized in that the original phase change absorbent is adopted to absorb CO in the flue gas2Absorbing CO2The phase separation is carried out on the solution, and the CO after the phase separation2The rich liquid is continuously used for treating CO in the flue gas2Absorbing, namely absorbing CO in the flue gas by adopting an original phase change absorbent2And using CO after phase separation2Rich liquid phase absorbing CO in flue gas2The process of (a) is carried out in different absorption columns.
2. The phase change absorbent as claimed in claim 1, which is suitable for absorbing CO in flue gas2Characterised by the fact that the reabsorption of CO is carried out2After CO2Desorbing the rich solution, and separating the desorbed solution from the phase-separated CO2The lean liquid phase is added after being mixed or used as an original phase change absorbent for recycling.
3. The phase change absorbent as claimed in claim 1, which is suitable for absorbing CO in flue gas2The method is characterized in that the phase change absorbent is an amine-organic solvent-water system phase change absorbent.
4. The phase change absorbent as claimed in claim 3, which is suitable for absorbing CO in flue gas2The method is characterized in that the phase change absorbent is ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water phase change absorbent.
5. The phase change absorbent as claimed in claim 1, which is suitable for absorbing CO in flue gas2The method of (1), wherein the viscosity of the original phase change absorbent is in the range of 2 to 10 mPas.
6. The phase change absorbent as claimed in claim 5, which is suitable for absorbing CO in flue gas2Characterized by the CO after phase separation2The viscosity of the rich liquid phase is in the range of 10-200 mPas.
7. The phase change absorbent as claimed in claim 1, which is suitable for absorbing CO in flue gas2The method is characterized in that the operating pressure of the different absorption towers is normal pressure, and the working temperature in the different absorption towers is 30-60 ℃.
8. Method according to any one of claims 1 to 7 for absorbing CO in flue gas by using a phase change absorbent2The absorption system is characterized by comprising a first absorption tower, a second absorption tower and a phase splitter, 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 exhaust 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 exhaust outlet of the second absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase splitter, a rich liquid phase outlet of the phase splitter is communicated with the absorbent inlet of the second absorption tower, the first absorption tower is used for absorption reaction of an original phase-change absorbent, and the second absorption tower is used for CO after phase splitting2Absorption reaction of rich liquid phase, and phase separator for absorbing CO2Phase separation of the latter original phase change absorbent.
9. The method as claimed in claim 8, wherein the phase change absorbent is used for absorbing CO in flue gas2Characterized in that it further comprises CO2A solution outlet of the second absorption tower is communicated with an inlet of the desorption device, a liquid phase outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, a lean liquid phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower, and the desorption device is used for absorbing CO again2After CO2And (4) desorbing the rich solution.
10. The method as claimed in claim 9, wherein the phase change absorbent is used for absorbing CO in flue gas2The absorption system is characterized in that a first conveying pump is installed on an absorbent conveying pipeline communicated with an absorbent inlet of the first absorption tower, and a second conveying pump is installed on a conveying pipeline between a rich liquid phase outlet of the phase separator and an absorbent inlet of the second absorption tower.
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