CN114405258B - Is suitable for low partial pressure CO 2 Capture-purified absorption system - Google Patents

Is suitable for low partial pressure CO 2 Capture-purified absorption system Download PDF

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CN114405258B
CN114405258B CN202111628965.1A CN202111628965A CN114405258B CN 114405258 B CN114405258 B CN 114405258B CN 202111628965 A CN202111628965 A CN 202111628965A CN 114405258 B CN114405258 B CN 114405258B
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tower
tail gas
liquid
enters
phase change
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CN114405258A (en
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陆诗建
刘玲
刘滋武
康国俊
闫新龙
王全德
黄飞
桑树勋
倪中海
朱家媚
王珂
李天泊
陈浮
陈润
刘世奇
王猛
朱前林
马静
郑司建
刘统
石付恒
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China University of Mining and Technology CUMT
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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
    • B01D53/79—Injecting reactants
    • 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
    • B01D53/343—Heat recovery
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B30/00—Heat pumps
    • F25B30/06—Heat pumps characterised by the source of low potential heat
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • 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

Abstract

The invention discloses a method suitable for low partial pressure CO 2 The trapping and purifying absorption system is a phase-change nano-fluid absorption system, the regenerated layered phase-change nano-absorbent consists of base liquid, a layering agent, an activating agent, nano-particles, a corrosion inhibitor and an antioxidant, the base liquid consists of hydroxyethyl ethylenediamine and tetraethylenepentamine, the layering agent consists of N-ethyl ethylenediamine and 1, 4-butanediamine, the activating agent consists of piperazine or diethanol amine, the nano-particles consist of copper oxide or magnesium oxide, the corrosion inhibitor consists of imidazoline benzoate-dimethyl sulfate quaternary ammonium salt or imidazoline benzoate-chloromethane quaternary ammonium salt, and the antioxidant consists of carbohydrazide or pyrogallol. The regenerative layered phase change nano absorbent can reduce the regeneration energy consumption and the regeneration temperature and improve the regeneration rate through the phase change in the regeneration process, has the characteristics of large absorption load, high absorption and desorption rates and low regeneration energy consumption, and can effectively reduce CO 2 Energy consumption capture and CO reduction 2 And (4) trapping cost.

Description

Is suitable for low partial pressure CO 2 Capture-purified absorption system
Technical Field
The invention relates to CO 2 A capture system, in particular to a system suitable for low partial pressure CO 2 An absorption system for trapping and purifying, which belongs to the technical field of flue gas purification.
Background
The CCUS (Carbon Capture, utilization and Storage) technology is a new development trend of the CCS (Carbon Capture and Storage) technology, namely, the CO discharged in the production process of emission sources of large-scale power plants, steel plants, chemical plants and the like 2 Collected and purified and then put into a new production process for recycling, rather than simply being sealed, as compared to CCSCCUS can convert CO 2 The resource utilization generates economic benefits and has more practical operability.
Coal is the most important energy type in China at present, and a coal-fired power plant is CO in China 2 The main emission source of the method can reach the CO in China 2 Over 50 percent of the total emission amount, and low partial pressure flue gas CO discharged by a coal-fired power plant 2 The key of carbon emission reduction in China is to carry out capture, recovery, utilization and sealing storage. CO2 2 Capture technique is the determination of CO in CCUS 2 The most critical links of the purity and the cost of resource utilization are that the energy consumption of the process accounts for more than 60 percent of the total energy consumption of the CCUS project, so that the energy consumption is reduced for the CO in the flue gas 2 The trapping is very important and is a technical bottleneck problem of key attack of CCUS large-scale popularization.
As shown in the following table, the current low partial pressure flue gas captures CO 2 The method comprises the methods of chemical absorption, physical absorption, membrane separation and the like, wherein the chemical absorption method is the most frequently selected flue gas CO in the CCUS project at present due to the technical maturity and the application prospect 2 A trapping method.
Figure BDA0003439636880000011
Figure BDA0003439636880000021
The chemical absorption method is to selectively mix CO in the flue gas with the absorbent 2 Chemical reaction to realize CO 2 Separated from other gases and regenerated by means of the reverse reaction of this reaction, releasing high-purity CO 2 And (4) carrying out enrichment. The reaction principle is that weak base and weak acid react to form water soluble salt which absorbs or releases CO 2 Is controlled by the chemical reaction equilibrium. The most important bottleneck limiting the large-scale application of the chemical absorption method at present is that the energy consumption is large and the cost is high.
In order to reduce energy consumption, researchers in the industry have conducted research in two major areas: the development of a high-efficiency absorbent absorption system and the capture process optimization of the capture system. Aiming at the absorbent, at present, there are several main types of absorbent, such as amine solution, ammonia water, caustic potash solution, ionic liquid and amino acid salt solution, etc., caustic potash solution and ionic liquid have high cost and are not easy to be used in large scale, while ammonia water is easy to volatilize and forms crystals to block pipelines, so that the mixed absorbent of different amines (ammonia) and novel phase change absorbent are the research focus of researchers in the industry at present. Aiming at the process optimization of the trapping system, the research focuses on an absorption system (a first type of phase-change absorption system) which is layered after absorption and an absorption system (a second type of phase-change absorption system) which is layered after desorption, and the regeneration energy consumption is reduced by reducing the regeneration liquid amount.
Disclosure of Invention
In view of the problems of the prior art, the invention provides a low partial pressure CO separating device 2 An absorption system for capturing and purifying, which can effectively reduce CO 2 Energy consumption capture and CO reduction 2 And (4) trapping cost.
To achieve the above purpose, the method is suitable for low partial pressure CO 2 The absorption system for trapping and purifying is a phase-change nano-fluid absorption system, the regenerated layered phase-change nano-absorbent of the phase-change nano-fluid absorption system consists of base liquid, a layering agent, an activating agent, nano particles, a corrosion inhibitor and an antioxidant, the base liquid consists of hydroxyethyl ethylenediamine and tetraethylenepentamine, the layering agent consists of N-ethyl ethylenediamine and 1, 4-butanediamine, the activating agent consists of piperazine or diethanolamine, the nano particles consist of copper oxide or magnesium oxide, the corrosion inhibitor consists of imidazoline benzoate-dimethyl sulfate quaternary ammonium salt or imidazoline benzoate-chloromethane quaternary ammonium salt, and the antioxidant consists of carbohydrazide or pyrogallol;
the total mass fraction of the regenerative stratified phase-change nano absorbent is 30wt%, and the proportions of the base liquid, the stratified agent, the activating agent, the nano particles, the corrosion inhibitor and the antioxidant are as follows: 15% -20%: 5% -9%: 1% -5%: 0.01% -0.05%: 0.025% -0.05%: 0.025 to 0.05 percent.
As an embodiment of the invention, the regenerative layered phase change nano-absorbent of the phase change nano-fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: copper oxide: benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt: carbohydrazide =15%:9%:5%:3%:3%:0.01%:0.05%:0.05 percent.
As an implementation mode of the invention, the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: n-ethyl ethylenediamine: 1, 4-butanediamine: diethanolamine: copper oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: pyrogallol =20%:5%:1%:5%:5%:0.05%:0.05%:0.05 percent.
As an embodiment of the invention, the regenerative layered phase change nano-absorbent of the phase change nano-fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: imidazoline benzoate-dimethyl sulfate quaternary ammonium salt: carbohydrazide =17%:7%:5%:1%:1%:0.03%:0.035%:0.035%.
As an implementation mode of the invention, the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: diethanolamine: magnesium oxide: benzoic acid imidazoline-chloromethane quaternary ammonium salt: pyrogallol =15%:9%:3%:2%:3%:0.035%:0.035%:0.035%.
As an implementation mode of the invention, the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: pyrogallol =17%:7%:4%:2%:3%:0.03%:0.025%:0.025 percent.
As an embodiment of the invention, the regenerative layered phase change nano-absorbent of the phase change nano-fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: n-ethyl ethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt: pyrogallol =16%:6%:3%:2%:3%:0.03%:0.035%:0.035%.
As an implementation mode of the invention, the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: carbohydrazide =18%:5%:4%:2%:3%:0.05%:0.04%:0.04 percent.
As an implementation mode of the invention, the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: n-ethyl ethylenediamine: 1, 4-butanediamine: diethanolamine: magnesium oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: carbohydrazide =17%:7%:3%:2%:3%:0.05%:0.04%:0.04 percent.
As an embodiment of the invention, the regenerative layered phase change nano-absorbent of the phase change nano-fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: n-ethyl ethylenediamine: 1, 4-butanediamine: piperazine: copper oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: carbohydrazide =17%:6%:4%:1%:2%:0.05%:0.04%:0.04 percent.
Compared with the prior art, the method is suitable for low partial pressure CO 2 The regenerative layered phase-change nano absorbent of the trapping and purifying absorption system can reduce the regeneration energy consumption and the regeneration temperature and improve the regeneration rate through phase change in the regeneration process, has the characteristics of large absorption load, high absorption and desorption rate and low regeneration energy consumption, and the self regeneration energy consumption of the absorbent is less than 2.7GJ/tCO 2 Can effectively reduce CO 2 Energy consumption capture and CO reduction 2 And (4) trapping cost.
Drawings
FIG. 1 is a schematic representation of a system for low partial pressure CO using phase change nanofluid absorption 2 An energy-saving process flow chart of trapping and purification.
In the figure: 1. a water washing pump, 2, a water washing tower, 3, an alkali pump, 4, a water washing liquid heat exchanger, 5, an induced draft fan, 6, an absorption tower, 7, an interstage cooler, 8, an interstage cooling pump, 9, a dry bed section, 10, a tail gas washing tower A,11, a tail gas washing liquid cooler A,12, a tail gas washing pump A,13, a tail gas washing liquid storage tank A,14, a tail gas washing tower B,15, a tail gas washing liquid cooler B,16, a tail gas washing pump B,17, a tail gas washing liquid storage tank B,18, a liquid distribution tank, 19, a rich liquid pump, 20, a regeneration tower, 21, a lean rich liquid heat exchanger, 22, a lean liquid cooler, 23, a condensed water heat exchanger, 24, a flash tank, 25, a flash pump, 26, a flash compressor, 27, a lean liquid pump, 28, a composite heat pump, 29, an evaporator A,30, an evaporator B,31, an absorber A, 32, an absorber B,33, a generator A,34, a generator B,35, a condenser A,36, a condenser B,37, a regeneration gas, a throttle valve, a condenser, 38, a condenser, 40, a boiling solution, a boiling water solution,
Detailed Description
The method is suitable for low partial pressure CO 2 The trapping and purifying absorption system is a phase-change nano-fluid absorption system, and the regenerative layered phase-change nano-absorbent of the phase-change nano-fluid absorption system consists of base liquid, a layering agent, an activating agent, nano-particles, a corrosion inhibitor and an antioxidant; the base liquid is a basic absorption liquid for ensuring the large load and high absorption rate of the absorbent and consists of hydroxyethyl ethylenediamine (AEEA) and tetraethylenepentamine (TETA); layering agent for regenerating CO in absorption system 2 The subsequent layering realizes the autonomous self-extraction of the organic phase, ensures large layering proportion and reduces energy consumption, and consists of N-ethyl ethylenediamine (N-ELDE) and 1, 4-Butanediamine (BDA); the activator is used for improving the absorption of CO by the absorption system 2 Reaction rate and desorption of CO 2 The reaction rate of (a) is composed of Piperazine (PZ) or Diethanolamine (DEA); the nano particles are used for strengthening mass transfer, improving the absorption rate and increasing the mass transfer absorption load and consist of copper oxide (CuO) or magnesium oxide (MgO); use of corrosion inhibitors forThe corrosion of an absorption system to steel (a reactor, heat exchange equipment, various storage tanks, pipelines and the like) is reduced, and the absorption system consists of benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt (IBDSQAS) or benzoic acid imidazoline-chloromethane quaternary ammonium salt (ICQAB); the antioxidant is used for reducing thermal degradation and oxidative degradation of the effective components of the absorbent and ensuring the stability of an absorption system and is composed of Carbohydrazide (CD) or pyrogallol (OTP). The total mass fraction of the regenerative layered phase-change nano absorbent of the phase-change nano fluid absorption system is 30wt%, and the proportions of the base liquid, the layering agent, the activating agent, the nano particles, the corrosion inhibitor and the antioxidant are as follows: 15% -20%: 5% -9%: 1% -5%: 0.01% -0.05%: 0.025% -0.05%: 0.025 to 0.05 percent.
Phase-change nanofluid absorption system-based low-partial-pressure CO absorption system 2 An energy-saving process for capturing and purifying adopts a coupling process of a graded flow system, an interstage cooling system, a combined heat pump system, an MVR flash evaporation heat pump system and a compression type heat pump system, as shown in figure 1, and is suitable for low-partial-pressure CO 2 The capturing and purifying system assembly comprises a water washing tower 2, an absorption tower 6, a regeneration tower 20, a flash tank 24 and a composite heat pump 28, wherein an evaporator, an absorber, a generator and a condenser are arranged in the composite heat pump 28, the input end of the generator is connected with an external steam source, and the output end of the generator is connected with the input end of a condensed water deoxygenator. To ensure the efficiency of the compound heat pump 28, the evaporator, the absorber, the generator, and the condenser may be provided as an evaporator a29 and an evaporator B30 connected in series, an absorber a31 and an absorber B32 connected in series, a generator a33 and a generator B34 connected in series, and a condenser a35 and a condenser B36 connected in series, respectively.
Suitable for low partial pressure CO 2 The energy-saving process for trapping and purifying specifically comprises the following parts:
a. washing with water: the washing tower 2 is provided with a washing liquid circulating device for circularly conveying washing liquid from bottom to top, the washing liquid circulating device comprises a washing pump 1 and a washing liquid heat exchanger 4, the washing liquid enters the washing liquid heat exchanger 4 for heat exchange through external circulating water after being pressurized by the washing pump 1, and enters the washing tower 2 for spraying after heat exchange (the temperature is reduced to 35-45 ℃); the alkali supplement amount of the washing liquid is controlled by a PH meter arranged on a circulating pipeline, the PH meter is interlocked with the alkali supplement pump 3, the output end of the alkali supplement pump 3 is communicated with the circulating pipeline, and the NaOH supplement amount is adjusted by adjusting the rotating speed of the alkali supplement pump 3 according to the feedback of the PH meter; flue gas discharged from a coal-fired power plant enters a washing tower 2 through a pipeline, is subjected to desulfurization, denitrification, dedusting and heat exchange by using washing liquid (the gas temperature is controlled to be 35-45 ℃), and is discharged from the top of the washing tower 2 and enters an induced draft fan 5.
b. Decarbonizing: the flue gas enters an absorption tower 6 from bottom to top after being pressurized by a draught fan 5, a barren liquor absorbent (with the temperature of 35-45 ℃) discharged by a barren liquor cooler 22 is sprayed into the absorption tower 6 from top to bottom and is in countercurrent contact with the barren liquor absorbent, and amine and CO 2 The amino carbonate (with the temperature of 45-55 ℃) generated by the reaction enters an interstage cooler 7 for exchanging heat through external circulating water to be cooled to 35-45 ℃, and enters an absorption tower 6 again after being pressurized by an interstage cooling pump 8 so as to improve the amine and CO 2 The decarburization reaction rate of (2).
c. Washing tail gas: a dry bed section 9 is arranged above the filler at the top of the absorption tower 6, the height of the filler of the dry bed section 9 is larger than 2m, the main function is to provide a cooling and condensing space for the tail gas discharged by the absorption tower 6, generally, moisture and organic amine in the tail gas discharged from a tail gas discharge port of the absorption tower 6 are in a supersaturated state, the moisture and the organic amine are cooled and condensed in the dry bed section 9 to form a liquid film with low amine concentration, the liquid film further generates gas-liquid equilibrium mass transfer with the flue gas, and most of the organic amine in the gas phase is recovered; the decarbonized gas passes through a dry bed section 9 at the top of an absorption tower 6 and is discharged through a tail gas discharge port at the top of the absorption tower 6 to enter a tail gas washing system, the tail gas washing system comprises a two-stage tail gas washing tower, the two-stage tail gas washing tower comprises a tail gas washing tower A10 and a tail gas washing tower B14 which are sequentially connected in series, enough growth space is mainly provided for aerosol to grow to 3 mu m or above, the conventional demister arranged on exhaust ports of the tail gas washing tower A10 and the tail gas washing tower B14 is matched to effectively remove organic amine in the form of aerosol, the tail gas washing tower A10 and the tail gas washing tower B14 are respectively provided with a tail gas washing liquid circulating device for circularly conveying tail gas washing liquid from the bottom to the top, the tail gas washing liquid circulating device of the tail gas washing tower A10 comprises a tail gas washing liquid storage tank A13, a tail gas washing liquid pump A12 and a tail gas washing liquid cooler A11, the tail gas washing liquid circulating device of the tail gas washing tower B14 comprises a tail gas washing liquid storage tank B17, a tail gas washing liquid pump B16 and a tail gas washing liquid cooler B15, the tail gas washing liquid tank and a tail liquid solution distribution tank 18 in the tail gas washing liquid distribution tank, and a tail gas washing liquid distribution tank balance liquid distribution tank in the tail gas washing liquid distribution system, and a poor absorption system is maintained, the tail gas washing liquid distribution tank 6 is maintained; the tail gas after being washed discharged from the tail gas washing tower B14 is discharged into a chimney.
d.CO 2 Desorption: absorb CO 2 The rich liquid of the gas is discharged from the bottom of the absorption tower 6, and is pressurized by a rich liquid pump 19 and then is conveyed in a grading way, wherein the first-stage rich liquid (the temperature of the rich liquid is 50-55 ℃) directly enters a first-stage spraying pipeline at the top of the regeneration tower 20, the second-stage rich liquid (the temperature of the rich liquid is 40-45 ℃) enters a second-stage rich liquid heat exchanger 21 for heat exchange and temperature rise, and the second-stage rich liquid (the temperature of the rich liquid is 95-105 ℃) enters a second-stage spraying pipeline of the regeneration tower 20 below the first-stage spraying pipeline after heat exchange; the third-stage rich liquid (the temperature of the rich liquid is 50-55 ℃) enters a third-stage rich liquid heat exchanger 23 for heat exchange and temperature rise through external steam condensed water, and the third-stage rich liquid (the temperature of the rich liquid is 95-105 ℃) enters a second-stage spraying pipeline of the regeneration tower 20 after heat exchange to realize CO 2 Desorption from the absorbent.
e. Flash evaporation heat supply: a liquid supplementing pipeline of the flash tank 24 is communicated with a pipeline from the secondary rich liquid heat exchanger 21 to the regeneration tower 20, so that a liquid supplementing process of the flash tank 24 is realized; the rich liquid (the temperature is 80-90 ℃) in the flash tank 24 is pressurized by a flash circulating pump 25 and then sequentially enters an absorber A31 and an absorber B32 of the compound heat pump 28 for heat exchange and temperature rise, and returns to the flash tank 24 for a flash process after the temperature rises to 90-100 ℃; the flash steam discharged from the top of the flash tank 24 enters a third-stage spray pipeline of the regeneration tower 20 below the second-stage spray pipeline after being pressurized by a flash compressor 26 (the temperature is 105-115 ℃) to provide heat for the solution regeneration process in the regeneration tower 20.
f. And (3) cyclic regeneration of the absorption solvent: the desorbed barren solution (with the temperature of 100-105 ℃) is pressurized by a barren solution outlet at the bottom of the regeneration tower 20 through a barren solution pump 27 and then divided into two-stage processes, wherein one stage of the barren solution enters a condenser A35 and a condenser B36 of the compound heat pump 28 in sequence for heat exchange and temperature rise, and enters a secondary spraying pipeline of the regeneration tower 20 again after the temperature rises to 105-115 ℃; the other stage as a heat exchange working medium of the secondary rich liquid heat exchanger 21 enters the secondary rich liquid heat exchanger 21 for heat exchange and temperature reduction, the temperature is reduced to 55-65 ℃, then the working medium sequentially enters an evaporator A29 and an evaporator B30 of the compound heat pump 28 for heat exchange and temperature reduction, the working medium enters the lean liquid cooler 22 for temperature reduction to be below 40 ℃ after the temperature is reduced to 40-50 ℃, and finally the working medium enters a spray pipeline of the absorption tower 6 to start a new absorption process, so that the cyclic regeneration of the absorption solvent is realized.
g. Treating regenerated gas: the regenerated gas (the temperature is more than 100 ℃) sucked out by rich liquor decomposition enters a regenerated gas compressor 37 from the outlet at the top of the regeneration tower 20 for pressurization (the temperature is raised to about 120-160 ℃), then enters a regenerator condenser 38 for condensation and cooling, and the condensation heat is transferred to the working medium of the heat pump; the cooled regeneration gas (the temperature is reduced to 80-90 ℃) enters a regeneration gas heat exchanger 42 for heat exchange and cooling through external circulating water, the temperature is reduced to 60-70 ℃, then the regeneration gas enters an air cooler 43 for continuous cooling to be below 40 ℃, finally the regeneration gas enters a gas-liquid separator 44 for gas-liquid separation, and the separated CO 2 The gas is used as product gas to enter a subsequent flow, and the separated dilute solution enters the tower kettle of the regeneration tower 20 after being pressurized by the reflux pump 45, so that the water balance of the system is maintained. In order to further realize energy conservation and consumption reduction, the input end of the external circulating water of the regenerated gas heat exchanger 42 is connected with the condensed water output end of the shaft seal heater of the generator set, and the output end of the external circulating water of the regenerated gas heat exchanger 42 is connected with the condensed water input end of the shaft seal heater of the generator set.
h. A compression heat pump cycle: the compression type heat pump system comprises a solution boiler 40, a heat pump working medium heating coil is arranged in the solution boiler 40, a lean solution input end at the lower part of the solution boiler 40 is connected with the tower kettle of the regeneration tower 20, and a gasification output end at the upper part of the solution boiler 40 is connected with a gasification input end at the lower part of the tower kettle of the regeneration tower 20; the heat pump working medium can adopt 141b, 123a, 507a and the like, the heat pump working medium in the regenerator condenser 38 absorbs the condensation heat of the regeneration gas, then is totally vaporized and overheated, then enters the heat pump working medium compressor 41 for heating and pressurizing, the high-temperature and high-pressure heat pump working medium enters the heat pump working medium heating coil in the solution boiler 40 to be used as a heat source to release the heat to the barren solution in the solution boiler 40, and the barren solution is gasified and then returns to the regeneration tower 20 through the gasification output end, the heat pump working medium is totally condensed into liquid, and then is cooled and depressurized through the throttle valve 39 to be returned to the regenerator condenser 38 for heating and next cycle. In order to achieve a better gasification effect, and enable the heat pump working medium to be completely condensed into liquid after flowing through the solution boiler 40, and further achieve energy conservation and consumption reduction, a steam heating coil connected with an external steam source can be arranged inside the solution boiler 40, the output end of the steam heating coil is connected with the input end of external circulating water of the tertiary rich liquid heat exchanger 23, the external steam source can supply hot steam to achieve a better gasification effect, meanwhile, the hot steam in the steam heating coil is condensed into water after heat exchange, the condensed water can be used as a heat exchange heating working medium of the tertiary rich liquid heat exchanger 23, and the condensed water can be recycled after being further cooled by the tertiary rich liquid heat exchanger 23 and deoxidized by a condensate deoxidizer.
The following steps are carried out to carry out CO treatment on the flue gas discharged by a certain coal-fired power plant 2 The present invention will be described with reference to the capture purification as an example.
The parameters of the absorption tower and the regeneration tower are shown in Table 1, the flue gas composition is shown in Table 2, and CO is 2 Trap purification experiment operating parameters are shown in table 3. Absorption tower and regenerator column all adopt stainless steel material and stainless steel ripple regular packing, and absorption tower, regenerator column and pipeline outside all wrap up insulation material, and the regeneration heat comes from the electric heater of regenerator column 20 bottom, adopts silicon controlled rectifier to adjust voltage control system's regeneration temperature.
TABLE 1 absorption and regeneration column parameters
Figure BDA0003439636880000081
TABLE 2 Smoke composition
Figure BDA0003439636880000082
TABLE 3 CO 2 Trapping and purifying experiment operating parameters
Figure BDA0003439636880000091
Example 1:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：CuO：IBDSQAS：CD＝15％：9％：5％：3％：3％： 0.01％：0.05％：0.05％。
the specific performance parameters of the conventional process and the energy-saving process are shown in tables 4 (a) and 4 (b).
Table 4 (a) table of performance parameters for example 1 using conventional process
Figure BDA0003439636880000092
Table 4 (b) table of performance parameters for example 1 using energy saving process
Figure BDA0003439636880000093
Example 2:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：DEA：CuO：ICQAB：OTP＝20％：5％：1％：5％：5％：0.05％：0.05％：0.05％。
the specific performance parameters of the conventional process and the energy-saving process are shown in tables 5 (a) and 5 (b).
TABLE 5 (a) TABLE of Performance parameters for example 2 using conventional process
Figure BDA0003439636880000101
TABLE 5 (b) TABLE of Performance parameters for example 2 with energy saving Process
Figure BDA0003439636880000102
Example 3:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：MgO：IBDSQAS：CD＝17％：7％：5％：1％：1％： 0.03％：0.035％：0.035％。
the specific performance parameters of the conventional process and the energy-saving process are shown in tables 6 (a) and 6 (b).
Table 6 (a) table of performance parameters for example 3 using conventional process
Figure BDA0003439636880000103
TABLE 6 (b) TABLE of Performance parameters for example 3 with energy saving Process
Figure BDA0003439636880000104
Example 4:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：DEA：MgO：ICQAB：OTP＝15％：9％：3％：2％：3％： 0.035％：0.035％：0.035％。
the specific performance parameters of the conventional process and the energy-saving process are shown in tables 7 (a) and 7 (b).
Table 7 (a) table of performance parameters for example 4 using conventional process
Figure BDA0003439636880000111
TABLE 7 (b) Performance parameters Table for example 4 with energy saving Process
Figure BDA0003439636880000112
Example 5:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：MgO：ICQAB：OTP＝17％：7％：4％：2％：3％： 0.03％：0.025％：0.025％。
the performance parameters of the energy-saving process are shown in table 8.
Table 8 table of performance parameters for example 5 using energy saving process
Figure BDA0003439636880000113
Example 6:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：MgO：IBDSQAS：OTP＝16％：6％：3％：2％： 3％：0.03％：0.035％：0.035％。
the performance parameters of the energy-saving process are shown in table 9.
Table 9 table of performance parameters of example 6 using energy saving process
Figure BDA0003439636880000114
Example 7:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：MgO：ICQAB：CD＝18％：5％：4％：2％：3％： 0.05％：0.04％：0.04％。
the performance parameters of the energy-saving process are shown in table 10.
Table 10 table of performance parameters for example 7 using energy saving process
Figure BDA0003439636880000121
Example 8:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：DEA：MgO：ICQAB：CD＝17％：7％：3％：2％：3％： 0.05％：0.04％：0.04％。
the performance parameters of the energy-saving process are shown in table 11.
Table 11 table of performance parameters of example 8 using energy saving process
Figure BDA0003439636880000122
Example 9:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：PZ：CuO：ICQAB：CD＝17％：6％：4％：1％：2％： 0.05％：0.04％：0.04％。
the performance parameters of the energy-saving process are shown in table 12.
Table 12 table of performance parameters for example 9 using energy saving process
Figure BDA0003439636880000123
Example 10:
the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
AEEA：TETA：N-ELDE：BDA：DEA：CuO：ICQAB：CD＝18％：5％：3％：2％：2％： 0.05％：0.04％：0.04％。
the performance parameters of the energy-saving process are shown in table 13.
Table 13 table of performance parameters for example 10 using energy saving process
Figure BDA0003439636880000131
The method is suitable for low partial pressure CO 2 The regenerated layered phase-change nano absorbent of the trapping and purifying absorption system can reduce the regeneration energy consumption and the regeneration temperature through phase change in the regeneration process, improve the regeneration rate, has the characteristics of large absorption load, high absorption and desorption rates and low regeneration energy consumption, and the self regeneration energy consumption of the absorbent is less than 2.7GJ/tCO 2 。
The low-partial-pressure CO coupling process adopting the coupling process of the graded flow system, the interstage cooling system, the combined heat pump system, the MVR flash evaporation heat pump system and the compression heat pump system is suitable for low-partial-pressure CO 2 The energy-saving process of trapping and purifying partially replaces the traditional regeneration process of 'a desorption tower and a boiler', can effectively reduce the volume of the boiler, greatly reduce the regeneration energy consumption, reduce the medicament loss and the degradation and deterioration of the medicament, improve the recycling frequency of the chemical absorbent, save the investment cost, realize the purposes of resource recovery and environmental pollution reduction, and ensure that CO can be recycled 2 The regeneration energy consumption of the trapping system is lower than 2.3GJ/tCO2. The composite absorption heat pump and MVR flash evaporation heat pump system can effectively recover the waste heat of the barren solution and is used for heating the rich solution, and compared with the regeneration energy consumption of the traditional process, the regeneration energy consumption can be reduced by 0.2-0.3 GJ/tCO2; the 'regeneration tower top compression heat pump system' can effectively recover regeneration tower top gas, and can reduce the regeneration energy consumption by 0.25-0.35 GJ/tCO2 compared with the regeneration energy consumption of the traditional process; by adopting the tail gas washing process of 'a dry bed and a two-stage tail gas washing tower', the dry bed can directly lead the organic amine to return to an absorption circulation system, the organic amine in the tail gas washing tower is slowly accumulated, the frequent water regulation and control can be effectively avoided, the three control links are favorable for the growth of aerosol, large particles can be effectively removed, the solvent loss is reduced, the emission of tail gas pollutants is reduced, and the absorption entrainment loss amount is less than 0.6kg/tCO 2 Compared with the traditional first-stage water washing process (about 1.0 kg/tCO) 2 ) The reduction can be more than 40%.

Claims (10)

1. Is suitable for low partial pressure CO 2 The absorption system is characterized by being a phase-change nano fluid absorption system, wherein a regenerated layered phase-change nano absorbent of the phase-change nano fluid absorption system consists of base liquid, a layering agent, an activating agent, nano particles, a corrosion inhibitor and an antioxidant, the base liquid consists of hydroxyethyl ethylenediamine and tetraethylenepentamine, the layering agent consists of N-ethyl ethylenediamine and 1, 4-butanediamine, the activating agent consists of piperazine or diethanolamine, the nano particles consist of copper oxide or magnesium oxide, the corrosion inhibitor consists of imidazoline benzoate-dimethyl sulfate quaternary ammonium salt or imidazoline benzoate-chloromethane quaternary ammonium salt, and the antioxidant consists of carbohydrazide or pyrogallol;
the total mass fraction of the regenerative layered phase change nano absorbent is 30wt%, and the proportions of the base liquid, the layering agent, the activating agent, the nano particles, the corrosion inhibitor and the antioxidant are as follows: 15% -20%: 5% -9%: 1% -5%: 0.01% -0.05%: 0.025-0.05%: 0.025 percent to 0.05 percent;
suitable for low partial pressure CO 2 Application of trapping and purifying absorption system to CO 2 CO capture and purification system assembly 2 When capturing and purifying, CO 2 The trapping and purifying system assembly comprises a water washing tower (2), an absorption tower (6), a regeneration tower (20), a flash tank (24) and a combined heat pump (28), wherein an evaporator, an absorber, a generator and a condenser are arranged in the combined heat pump (28), the evaporator, the absorber, the generator and the condenser are respectively provided with an evaporator A (29) and an evaporator B (30) which are connected in series, an absorber A (31) and an absorber B (32) which are connected in series, a generator A (33) and a generator B (34) which are connected in series, a condenser A (35) and a condenser B (36) which are connected in series, and CO is carried out 2 The trapping purification specifically comprises the following parts:
a. washing with water: flue gas enters a washing tower (2) through a pipeline, is discharged from the top of the washing tower (2) and enters a draught fan (5) after being subjected to desulfurization, denitrification, dedusting and heat exchange by washing liquid, and the gas temperature of the flue gas discharged from the top of the washing tower (2) is controlled to be 35-45 ℃;
b. decarbonization: flue gas enters an absorption tower (6) from bottom to top after being pressurized by a draught fan (5), a barren liquor absorbent discharged by a barren liquor cooler (22) is sprayed from top to bottom to enter the absorption tower (6), the barren liquor absorbent and the absorption tower are in countercurrent contact for decarburization reaction, and the temperature of the barren liquor absorbent discharged by the barren liquor cooler (22) and entering the absorption tower (6) is controlled to be 35-45 ℃;
c. washing tail gas: the decarbonized gas passes through a dry bed section (9) at the top of an absorption tower (6) and is discharged through a tail gas discharge port at the top of the absorption tower (6) to enter a tail gas washing system, the tail gas washing system comprises two stages of tail gas washing towers, the two stages of tail gas washing towers comprise a tail gas washing tower A (10) and a tail gas washing tower B (14) which are sequentially connected in series, demisters are arranged on exhaust ports of the tail gas washing tower A (10) and the tail gas washing tower B (14), the tail gas washing tower A (10) and the tail gas washing tower B (14) are respectively provided with a tail gas washing liquid circulating device for circularly conveying tail gas washing liquid from bottom to top, the tail gas washing liquid circulating device of the tail gas washing tower A (10) comprises a tail gas washing liquid storage tank A (13), a tail gas washing liquid pump A (12) and a tail gas washing liquid cooler A (11), the tail gas washing liquid circulating device of the tail gas washing tower B (14) comprises a tail gas storage tank B (17), a tail gas washing liquid pump B (16) and a tail gas washing liquid cooler B (15), tail gas washing liquid recycling device of the tail gas washing liquid enters a tail liquid storage tank (18) after passing through a tail gas washing liquid tank (18), and an aerosol recovery tank, the tail gas washing liquid washing tank B washing tank (18) of the tail gas washing tower returns to the absorption tower;
d.CO 2 desorbing: absorb CO 2 The rich liquid of the gas is discharged from the bottom of the absorption tower (6), and is pressurized by a rich liquid pump (19) and then is conveyed in a grading way, wherein the primary rich liquid directly enters a primary spray pipeline at the top of the regeneration tower (20), the secondary rich liquid enters a secondary rich liquid heat exchanger (21) for heat exchange and temperature rise, the heat exchange and temperature rise temperature is controlled to be 95-105 ℃, and the secondary rich liquid enters a secondary spray pipeline of the regeneration tower (20) below the primary spray pipeline after heat exchange; the third-stage rich liquid enters a third-stage rich liquid heat exchanger (23) for heat exchange and temperature rise through external circulating water, the temperature of the heat exchange and temperature rise is controlled to be 95-105 ℃, and the third-stage rich liquid enters a second-stage spraying pipeline of the regeneration tower (20) after heat exchange;
e. flash evaporation heat supply: a liquid supplementing pipeline of the flash tank (24) is communicated with a pipeline leading to the regeneration tower (20) from the secondary rich liquid heat exchanger (21); the rich liquid in the flash tank (24) is pressurized by a flash circulating pump (25) and then enters an absorber of a composite heat pump (28) for heat exchange and temperature rise, the temperature of the heat exchange and temperature rise is controlled to be 90-100 ℃, and the rich liquid returns to the flash tank (24) for flash evaporation after temperature rise; the flash steam discharged from the top of the flash tank (24) is pressurized by a flash compressor (26), the temperature is controlled to be 105-115 ℃ after pressurization, and the flash steam enters a third-stage spraying pipeline of the regeneration tower (20) below a second-stage spraying pipeline;
f. and (3) cyclic regeneration of the absorption solvent: the desorbed barren solution is pressurized by a barren solution pump (27) from a barren solution outlet at the bottom of the regeneration tower (20) and then divided into two-stage processes, wherein the first stage enters a condenser of a compound heat pump (28) for heat exchange and temperature rise, the temperature is controlled to be 105-115 ℃ after temperature rise, and the barren solution enters a secondary spray pipeline of the regeneration tower (20) again; the other stage of the heat exchange working medium as the heat exchange working medium of the secondary rich liquid heat exchanger (21) enters the secondary rich liquid heat exchanger (21) for heat exchange and cooling, the temperature is controlled to be 55-65 ℃ after heat exchange and cooling, then the heat exchange and cooling are continuously carried out in an evaporator of the composite heat pump (28), the temperature is controlled to be 40-50 ℃ after heat exchange and cooling, then the heat exchange and cooling are continuously carried out in a lean liquid cooler (22), and finally the heat exchange and cooling enters a spray pipeline of an absorption tower (6) to start a new absorption process;
g. treating regenerated gas: the regenerated gas sucked out by the rich liquor decomposition enters a regenerated gas compressor (37) from an outlet at the top of a regeneration tower (20) for pressurization, the temperature is controlled to be 120-160 ℃ after pressurization, and then the regenerated gas enters a regenerator condenser (38) for condensation and cooling to 80-90 ℃, and the condensation heat is transferred to a heat pump working medium; the cooled regeneration gas enters a regeneration gas heat exchanger (42) for heat exchange and cooling through external circulating water, the temperature is reduced to 60-70 ℃, then the regeneration gas enters an air cooler (43) for continuous cooling to below 40 ℃, finally the regeneration gas enters a gas-liquid separator (44) for gas-liquid separation, and the separated CO 2 The gas is used as product gas to enter a subsequent flow, and the separated dilute solution enters a tower kettle of a regeneration tower (20) after being pressurized by a reflux pump (45);
h. a compression heat pump cycle: the compression type heat pump system comprises a solution boiler (40), a heat pump working medium heating coil is arranged in the solution boiler (40), a solution input end at the lower part of the solution boiler (40) is connected with a tower kettle of the regeneration tower (20), and a gasification output end at the upper part of the solution boiler (40) is connected with a gasification input end at the lower part of the tower kettle of the regeneration tower (20); the heat pump working medium in the regenerator condenser (38) absorbs the condensation heat of the regenerated gas, then is completely vaporized and superheated, then enters a heat pump working medium compressor (41) for heating and pressurizing, the heat pump working medium with high temperature and high pressure enters a heat pump working medium heating coil in a solution boiler (40), the solution is vaporized and then returns to the regeneration tower (20) through a vaporization output end, and the heat pump working medium condensed into liquid is cooled and depressurized through a throttle valve (39) and then returns to the regenerator condenser (38) for heating and next cycle.
2. The method of claim 1 for low partial pressure CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: copper oxide: benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt: carbohydrazide =15%:9%:5%:3%:3%:0.01%:0.05%:0.05 percent.
3. The method of claim 1 adapted for low partial pressure of CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: diethanolamine: copper oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: pyrogallol =20%:5%:1%:5%:5%:0.05%:0.05%:0.05 percent.
4. The method of claim 1 for low partial pressure CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt: carbohydrazide =17%:7%:5%:1%:1%:0.03%:0.035%:0.035%.
5. The method of claim 1 for low partial pressure CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: diethanolamine: magnesium oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: pyrogallol =15%:9%:3%:2%:3%:0.035%:0.035%:0.035%.
6. The method of claim 1 for low partial pressure CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: pyrogallol =17%:7%:4%:2%:3%:0.03%:0.025%:0.025 percent.
7. The method of claim 1 adapted for low partial pressure of CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: imidazoline benzoate-dimethyl sulfate quaternary ammonium salt: pyrogallol =16%:6%:3%:2%:3%:0.03%:0.035%:0.035 percent.
8. The method of claim 1 adapted for low partial pressure of CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: piperazine: magnesium oxide: benzoic acid imidazoline-chloromethane quaternary ammonium salt: carbohydrazide =18%:5%:4%:2%:3%:0.05%:0.04%:0.04 percent.
9. The method of claim 1 adapted for low partial pressure of CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: N-Ethylethylenediamine: 1, 4-butanediamine: diethanolamine: magnesium oxide: benzoic acid imidazoline-chloromethane quaternary ammonium salt: carbohydrazide =17%:7%:3%:2%:3%:0.05%:0.04%:0.04 percent.
10. The method of claim 1 for low partial pressure CO 2 The trapping and purifying absorption system is characterized in that the regenerative layered phase change nano absorbent of the phase change nano fluid absorption system comprises the following components in percentage by mass:
hydroxyethyl ethylenediamine: tetraethylenepentamine: n-ethyl ethylenediamine: 1, 4-butanediamine: piperazine: copper oxide: benzoic acid imidazoline-methyl chloride quaternary ammonium salt: carbohydrazide =17%:6%:4%:1%:2%:0.05%:0.04%:0.04 percent.
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