Application system of carbon dioxide absorbent

Abstract

The utility model discloses an application system of a carbon dioxide absorbent, relates to the technical field of absorbents, and discloses a novel phase change type CO2 absorbent prepared by mixing ionic liquid hydroxyethyl ethylenediamine imidazole-amino acid serving as a main absorbent, ethanolamine / piperazine serving as an accelerant, n-butyl alcohol serving as a phase splitting agent and a certain amount of water. The absorption capacity is high, the regeneration energy consumption can be greatly reduced while the absorption efficiency is ensured, and the stability is good; meanwhile, the carbon capture performance testing device is designed into a movable skid-mounted type, and the two-phase separator which is wide at the upper part and narrow at the lower part is utilized, so that phase splitting can be quickly realized, the device can be easily connected with an industrial production side line, and the industrial performance of the absorbent can be quickly verified.

Description

Technical Field

[0001] This application relates to the technical field of absorbents, and in particular to an application system for a carbon dioxide absorbent. Background Technology

[0002] Currently, the most widely used CO2 capture technology in industry is the amine solution absorption method, with monoethanolamine (MEA) being the most common commercial absorbent. MEA has high absorption capacity and good selectivity, but its regeneration energy consumption is high, and the amine component is prone to thermal and oxidative degradation during heating. Studies have shown that reducing the water content in the MEA solution from 70% to 60% can reduce the regeneration energy consumption from 3.29 GJ to 3.01 GJ / tCO2. Excessively high regeneration energy consumption significantly increases the operating cost of CO2 capture technology, thus limiting its industrial application.

[0003] Compared with traditional amine solution absorbents, ionic liquid materials have advantages such as low regeneration energy consumption, good water resistance, and low corrosivity, and have broad application prospects in the adsorption field. However, ionic liquids also face problems such as high viscosity of the rich phase and difficulty in regeneration. In terms of reducing regeneration energy consumption, liquid-liquid phase change solvents have broad development prospects. Liquid-liquid phase change absorbents can reduce the volume of the regenerated rich phase, and after coupling with energy-saving processes, they can significantly reduce carbon capture energy consumption. Related research has become a key focus in the development of new carbon capture technologies. How to reduce the viscosity of ionic liquid absorbents and combine the advantages of phase change absorbents to ensure absorption efficiency while significantly reducing regeneration energy consumption is the current research direction for absorbents.

[0004] Therefore, in order to solve the above-mentioned problems, there is an urgent need to provide a new type of phase change CO2 absorbent. Utility Model Content

[0005] The purpose of this application is to provide an application system for carbon dioxide absorbents to solve the problems of high viscosity, difficult regeneration, and poor stability of existing ionic liquid absorbents.

[0006] This application provides a carbon dioxide absorbent application system using the following technical solution:

[0007] An application system for a carbon dioxide absorbent, wherein the carbon dioxide absorbent is used to test its absorbent performance using a carbon capture performance testing device, the carbon capture performance testing device comprising a laboratory absorption-desorption device and an industrial pilot-scale device;

[0008] The industrial pilot-scale device includes an absorption tower, which is connected to an absorbent storage structure and a raw material gas storage structure. The gas output end of the top of the absorption tower is connected to a first gas-liquid separator, the gas output end of the first gas-liquid separator is connected to a first gas analyzer, and the liquid output end of the first gas-liquid separator is connected to the liquid input end of the absorption tower.

[0009] The liquid output end at the bottom of the absorption tower is connected to a two-phase separator. The upper output end of the two-phase separator is connected to the gas input end at the top of the absorption tower through a first conveying mechanism. The lower output end of the two-phase separator is connected to a lean-rich liquid heat exchanger through a second conveying mechanism.

[0010] The liquid output end of the lean-rich liquid heat exchanger is connected to a desorption tower, the desorption tower is connected to a reboiler, the gas output end of the desorption tower is connected to a second gas-liquid separator, the gas output end of the second gas-liquid separator is connected to a second gas analyzer, and the liquid output end of the second gas-liquid separator is connected to the liquid input end of the desorption tower.

[0011] The liquid output end of the reboiler is connected to the liquid input end of the lean-rich liquid heat exchanger via a third conveying mechanism, and the liquid output end of the lean-rich liquid heat exchanger is connected to the liquid input end at the top of the absorption tower via a fourth conveying mechanism.

[0012] Furthermore, the first conveying mechanism includes a first conveying pipe connected between the two-phase separator and the absorption tower, and a lean phase pump is installed on the first conveying pipe.

[0013] Furthermore, the second conveying mechanism includes a second conveying pipe connected between the two-phase separator and the lean and rich liquid heat exchanger, and a rich liquid pump is installed on the second conveying pipe.

[0014] Furthermore, the third conveying mechanism includes a third conveying pipe connected between the reboiler and the lean and rich liquid heat exchanger, and a lean liquid pump is installed on the third conveying pipe.

[0015] Furthermore, a first cooler is connected between the gas output end of the desorption tower and the gas input end of the second gas-liquid separator.

[0016] Furthermore, the fourth conveying mechanism includes a fourth conveying pipe connected between the lean and rich liquid heat exchanger and the absorption tower, and a lean liquid cooling pump and a cooler are sequentially installed on the fourth conveying pipe.

[0017] Furthermore, flow meters are connected between the first gas-liquid separator and the first gas analyzer, and between the second gas-liquid separator and the second gas analyzer.

[0018] Furthermore, the two-phase separator has an overall cone-shaped structure that is wider at the top and narrower at the bottom, and the material of the two-phase separator is transparent plexiglass.

[0019] Compared with the prior art, the beneficial effects of this application are as follows:

[0020] A novel phase-change CO2 absorbent, prepared by mixing ionic liquid hydroxyethyl ethylenediamine imidazole-amino acid as the main absorbent, ethanolamine / piperazine as the promoter, n-butanol as the phase-separating agent, and a certain amount of water, not only has high absorption capacity and ensures absorption efficiency but also significantly reduces regeneration energy consumption and has good stability.

[0021] Meanwhile, by designing the carbon capture performance testing device as a movable skid-mounted unit and utilizing a two-phase separator that is wider at the top and narrower at the bottom, phase separation can be quickly achieved, making it easy to connect to industrial production lines and thus enabling rapid industrial performance verification of the absorbent. Attached Figure Description

[0022] Figure 1 This is a flowchart of the industrial test apparatus according to an embodiment of this application.

[0023] Figure 2 This is a schematic diagram of the laboratory absorption-desorption device according to an embodiment of this application.

[0024] Explanation of reference numerals in the attached figures:

[0025] 1. Absorption tower; 2. First gas-liquid separator; 3. First gas analyzer; 4. Two-phase separator; 5. Lean and rich liquid heat exchanger; 6. Desorption tower; 7. Reboiler; 8. Second gas-liquid separator; 9. Second gas analyzer; 10. Gas pipe; 11. Liquid pipe; 12. Flow meter; 13. First delivery pipeline; 14. Lean phase pump; 15. Second delivery pipeline; 16. Rich liquid pump; 17. First cooler; 18. Third delivery pipeline; 19. Lean liquid pump; 20. Fourth delivery pipeline; 21. Lean liquid cooling pump; 22. Second cooler; 23. CO2 / N2 mixed gas cylinder; 24. CO2 absorption structure; 25. U-shaped drying structure; 26. CO2 analyzer; 27. Tail gas absorption structure; 28. Mass flow meter. Detailed Implementation

[0026] The following is in conjunction with the appendix Figure 1-2 This application will be described in further detail.

[0027] On one hand, this application discloses a carbon dioxide absorbent, which is composed of a main absorbent, an accelerator, a phase-separating agent, and water. In this embodiment, the main absorbent is a hydroxyethyl ethylenediamine imidazole-amino acid ionic liquid, the accelerator is ethanolamine / piperazine, and the phase-separating agent is n-butanol. This novel phase-change CO2 absorbent, prepared by mixing the ionic liquid hydroxyethyl ethylenediamine imidazole-amino acid as the main absorbent, ethanolamine / piperazine as the accelerator, n-butanol as the phase-separating agent, and a certain amount of water, not only has high absorption capacity and ensures absorption efficiency while significantly reducing regeneration energy consumption, but also exhibits good stability.

[0028] On the other hand, this application also provides an application system for a carbon dioxide absorbent, which includes the application of the carbon dioxide absorbent to perform absorbent performance testing through a carbon capture performance testing device, wherein the carbon capture performance testing device is a movable skid-mounted structure.

[0029] Reference Figure 1 In this embodiment, the carbon capture performance testing device includes a laboratory absorption-desorption device and an industrial test device. Thus, the CO2 capture performance of the novel phase change CO2 absorbent prepared above is evaluated using both the laboratory absorption-desorption device and the industrial test device.

[0030] Specifically, refer to Figure 1 In this embodiment, the industrial test apparatus includes an absorption tower 1, a first gas-liquid separator 2, a first gas analyzer 3, a two-phase separator 4, a first conveying mechanism, a second conveying mechanism, a lean-rich liquid heat exchanger 5, a desorption tower 6, a reboiler 7, a second gas-liquid separator 8, a second gas analyzer 9, a third conveying mechanism, and a fourth conveying mechanism.

[0031] The inlet on one side of the top of the absorption tower 1 is connected to the absorbent storage structure via a pipeline and a delivery pump. The absorbent storage structure stores the novel phase change CO2 absorbent prepared above. When the pipeline and delivery pump are started, the novel phase change CO2 absorbent is pumped to the top of the absorption tower 1.

[0032] Meanwhile, the inlet on one side of the bottom of the absorption tower 1 is connected to the raw material gas storage structure via a pipeline and an induced draft fan. The raw material gas storage structure stores raw material gas, which is biogas or flue gas. When the pipeline and induced draft fan are activated, the raw material gas is drawn into the bottom of the absorption tower 1. This allows the raw material gas and the novel phase change CO2 absorbent to come into countercurrent contact within the absorption tower 1, thereby completing the absorption between the gas and the absorbent.

[0033] Additionally, refer to Figure 1In this embodiment, the first gas-liquid separator 2 is disposed on one side of the top of the absorption tower 1. The gas inlet of the first gas-liquid separator 2 is connected to the gas outlet of the top of the absorption tower 1 via a gas pipe 10, so that the liquid-containing gas after absorption in the absorption tower 1 is transported along the gas pipe 10 into the first gas-liquid separator 2 for gas-liquid separation. Furthermore, the liquid outlet of the first gas-liquid separator 2 is connected to the liquid inlet of the top of the absorption tower 1 via a liquid pipe 11, so that the separated liquid in the first gas-liquid separator 2 flows back into the absorption tower 1 along the liquid pipe 11, allowing the liquid to absorb CO2.

[0034] Meanwhile, the first gas analyzer 3 is located on one side of the first gas-liquid separator 2. The gas input end of the first gas analyzer 3 is connected to the gas output end of the first gas-liquid separator 2, so that the gas dried after gas-liquid separation in the first gas-liquid separator 2 is discharged into the first gas analyzer 3, and then the concentration of CO2 is analyzed and tested using the first gas analyzer 3. Preferably, in this embodiment, a flow meter 12 is connected between the first gas-liquid separator 2 and the first gas analyzer 3; by setting the flow meter 12, the flow rate of the gas discharged from the first gas-liquid separator 2 can be measured.

[0035] Reference Figure 1 In this embodiment, the two-phase separator 4 is located on one side of the bottom of the absorption tower 1. The liquid inlet of the two-phase separator 4 is connected to the liquid outlet of the bottom of the absorption tower 1 via a liquid pipe 11, allowing the liquid absorbing CO2 in the absorption tower 1 to enter the two-phase separator 4. The two-phase separator 4 has a cone-shaped structure that is wider at the top and narrower at the bottom, enabling rapid liquid phase separation. This results in the rich phase accumulating in the lower layer of the two-phase separator 4, while the lean phase is located in the upper layer. Preferably, in this embodiment, the two-phase separator 4 is made of transparent plexiglass, allowing observation of the phase separation of the rich and lean phases during the experiment, thus facilitating process adjustments.

[0036] In addition, in this embodiment, the upper output end of the two-phase separator 4 is connected to the gas input end at the top of the absorption tower 1 through the first conveying mechanism; the first conveying mechanism is used to transport the lean phase of the upper layer of the two-phase separator 4 into the interior of the absorption tower 1 so as to achieve the effect of continuing to absorb gas.

[0037] Specifically, refer to Figure 1In this embodiment, the first conveying mechanism includes a first conveying pipe 13 and a lean phase pump 14. One end of the first conveying pipe 13 is connected to the upper output end of the two-phase separator 4, and the other end is connected to the gas input end at the top of the absorption tower 1. The lean phase pump 14 is installed on the first conveying pipe 13. When the lean phase pump 14 is started, the first conveying pipe 13 can extract the lean phase from the upper layer of the two-phase separator 4, and then use the first conveying pipe 13 to uniformly transport the lean phase back into the absorption tower 1.

[0038] Meanwhile, the lean-rich liquid heat exchanger 5 is located on one side of the two-phase separator 4. The liquid inlet of the lean-rich liquid heat exchanger 5 and the lower outlet of the two-phase separator 4 are connected to each other through a second conveying mechanism. The second conveying mechanism facilitates the transport of the rich phase liquid in the lower layer of the two-phase separator 4 to the interior of the lean-rich liquid heat exchanger 5, and then the rich phase liquid is heat-exchanged by the lean-rich liquid heat exchanger 5.

[0039] Specifically, refer to Figure 1 In this embodiment, the second conveying mechanism includes a second conveying pipe 15 and a rich liquid pump 16. One end of the second conveying pipe 15 is connected to the lower output end of the two-phase separator 4, and the other end is connected to the liquid input end of the lean-rich liquid heat exchanger 5. The rich liquid pump 16 is installed on the second conveying pipe 15. When the rich liquid pump 16 is started, the second conveying pipe 15 draws the rich phase liquid from the lower layer of the two-phase separator 4, and then uses the second conveying pipe 15 to uniformly transport the rich phase liquid to the interior of the lean-rich liquid heat exchanger 5.

[0040] In addition, refer to Figure 1 In this embodiment, the desorption tower 6 is located on the side of the lean-rich liquid heat exchanger 5 away from the absorption tower 1. The liquid inlet at the top of the desorption tower 6 is connected to the liquid outlet of the lean-rich liquid heat exchanger 5 via a liquid pipe 11. When the rich liquid pump 16 is started, the rich phase liquid after heat exchange is pumped into the interior of the desorption tower 6 along the liquid pipe 11. A reboiler 7 is connected to the bottom of the desorption tower 6. After the desorption tower 6 is heated to a certain temperature by the reboiler 7, CO2 is desorbed from the rich phase liquid inside the desorption tower 6.

[0041] In this embodiment, the second gas-liquid separator 8 is disposed on one side of the top of the desorption tower 6. The gas inlet of the second gas-liquid separator 8 is connected to the gas outlet of the top of the desorption tower 6 via a gas pipe 10, so that the liquid-containing CO2 gas desorbed in the desorption tower 6 is transported into the second gas-liquid separator 8 along the gas pipe 10 for gas-liquid separation. Preferably, a first cooler 17 is also connected to the gas pipe 10 between the gas outlet of the desorption tower 6 and the gas inlet of the second gas-liquid separator 8; the first cooler 17 is used to condense the liquid-containing CO2 gas, and finally the condensed liquid-containing CO2 gas is discharged into the second gas-liquid separator 8 for gas-liquid separation.

[0042] Furthermore, the second gas analyzer 9 is located on one side of the second gas-liquid separator 8. The gas input end of the second gas analyzer 9 is connected to the gas output end of the second gas-liquid separator 8, so that the gas dried after gas-liquid separation in the second gas-liquid separator 8 is discharged into the second gas analyzer 9, and then the concentration of CO2 is analyzed and tested using the second gas analyzer 9. Preferably, in this embodiment, a flow meter 12 is connected between the second gas-liquid separator 8 and the second gas analyzer 9; by setting the flow meter 12, the flow rate of the gas discharged from the second gas-liquid separator 8 can be measured.

[0043] Furthermore, the liquid output end of the second gas-liquid separator 8 is connected to the liquid input end at the top of the desorption tower 6 via a liquid pipe 11, allowing the separated liquid in the second gas-liquid separator 8 to flow back into the desorption tower 6 along the liquid pipe 11. Simultaneously, the liquid output end of the reboiler 7 is connected to the liquid input end of the lean-rich liquid heat exchanger 5 via a third conveying mechanism, and the liquid output end of the lean-rich liquid heat exchanger 5 is connected to the liquid input end at the top of the absorption tower 1 via a fourth conveying mechanism.

[0044] This allows the rich phase liquid after desorption to enter the reboiler 7 from the desorption tower 6, and then be transported to the lean and rich liquid heat exchanger 5 for heat exchange treatment under the action of the third conveying mechanism. After heat exchange, the rich phase liquid enters the absorption tower 1 through the fourth conveying mechanism to continue absorbing CO2.

[0045] The structure of the third and fourth conveying mechanisms is described in detail below:

[0046] Specifically, refer to Figure 1In this embodiment, the third conveying mechanism includes a third conveying pipe 18 and a lean liquid pump 19. One end of the third conveying pipe 18 is connected to the liquid output end of the reboiler 7, and the other end is connected to the liquid input end of the lean-rich liquid heat exchanger 5. The lean liquid pump 19 is installed on the third conveying pipe 18. When the lean liquid pump 19 is started, the third conveying pipe 18 extracts the rich phase liquid after desorption from the reboiler 7, and then uses the third conveying pipe 18 to uniformly transport the rich phase liquid to the interior of the lean-rich liquid heat exchanger 5.

[0047] Specifically, refer to Figure 1 In this embodiment, the fourth conveying mechanism includes a fourth conveying pipe 20, a lean liquid cooling pump 21, and a second cooler 22. One end of the fourth conveying pipe 20 is connected to the liquid output end of the lean and rich liquid heat exchanger 5, and the other end of the fourth conveying pipe 20 is connected to the liquid input end at the top of the absorption tower 1. The lean liquid cooling pump 21 and the second cooler 22 are respectively installed sequentially on the fourth conveying pipe 20 along the liquid conveying direction.

[0048] When the lean liquid cooling pump 21 is started, the fourth delivery pipe 20 draws out the rich phase liquid after heat exchange in the lean and rich liquid heat exchanger 5, and then uses the fourth delivery pipe 20 to uniformly transport the rich phase liquid to the inside of the absorption tower 1, so that the rich phase liquid continues to absorb CO2 in the absorption tower 1; and during the transportation process, the rich phase liquid is cooled down by the second cooler 22.

[0049] Preferably, in this embodiment, multiple pressure indicators, pressure transmitters, temperature indicators, and temperature transmitters are also installed in the entire carbon capture performance testing device; with the cooperation of these indicators and transmitters, the temperature and pressure of the entire testing device can be effectively monitored, thereby ensuring the accuracy and safety of the entire testing device.

[0050] Therefore, this application designs the carbon capture performance testing device as a movable skid-mounted type, and utilizes a two-phase separator 4 that is wider at the top and narrower at the bottom, which enables rapid phase separation and easy connection to industrial production lines, thereby enabling rapid industrial performance verification of the absorbent.

[0051] Secondly, refer to Figure 1 In this embodiment, the laboratory absorption-desorption device is measured using a bubbling absorption and heating desorption device. The specific testing steps are as follows: the mixed gas is absorbed to near saturation through the bubbling absorption device; this mixed gas consists of 85% CO2 and 15% N2; and absorption stops when the CO2 concentration in the outlet gas is between 13-14%. The desorption process involves heating the gas to a certain temperature using a heating desorption device, maintaining this temperature for a period of time, and then measuring the desorption efficiency.

[0052] Specifically, refer to Figure 2 In this embodiment, the bubbling absorption device includes a CO2 / N2 mixed gas cylinder 23, a CO2 absorption structure 24, a U-shaped drying structure 25, a CO2 analyzer 26, and a tail gas absorption structure 27. The CO2 / N2 mixed gas cylinder 23, CO2 absorption structure 24, U-shaped drying structure 25, CO2 analyzer 26, and tail gas absorption structure 27 are connected to each other in pairs via gas pipes 10.

[0053] When the CO2 / N2 mixed gas cylinder 23 delivers the mixed gas into the CO2 absorption structure 24 to absorb CO2, the absorbed CO2 gas is then delivered to the U-shaped drying structure 25 for drying. The dried gas is then detected by the CO2 analyzer 26 and finally delivered to the tail gas absorption structure 27 for effective treatment.

[0054] Meanwhile, a mass flow meter 28 is installed on the gas pipe 10 between the CO2 / N2 mixed gas cylinder 23 and the CO2 absorption structure 24 to directly determine the flow rate of the mixed gas by measuring the mass of the mixed gas. Specifically, this heating desorption device has a structure basically the same as the bubble absorption device described above, except that the heating desorption device does not have the CO2 / N2 mixed gas cylinder 23.

[0055] Secondly, this application provides a method for preparing a carbon dioxide absorbent, including the following preparation method:

[0056] (1) Synthesis of hydroxyethyl ethylenediamine imidazole-amino acid ionic liquid:

[0057] First, equimolar amounts of N-butylimidazole and hydrobromide are mixed in a reactor, dissolved in anhydrous ethanol, and then equimolar amounts of hydroxyethyl ethylenediamine are added. The mixture is stirred for 24 hours to allow the mixture to undergo addition and ion exchange reactions.

[0058] The regenerated ion exchange resin was then soaked in NaOH and packed into an ion exchange column to perform ion exchange, yielding an ethanol solution of [AEEAIm][OH]. An equimolar amount of an amino acid salt was then added; specifically, the amino acid salt was one of lysine, alanine, or arginine. The mixture was then neutralized at room temperature for 24-28 hours, and ethanol and water were removed by vacuum distillation. The solution was then dried under vacuum at 80°C for 48 hours to obtain the [AEEAIm][AA] ionic liquid.

[0059] (2) Preparation of phase change absorbent:

[0060] In this embodiment, the phase change absorbent comprises an ionic liquid [AEEAIm][AA], a promoter, a phase-separating agent, and water. The specific preparation method is as follows:

[0061] Example 1:

[0062] First, a certain amount of the prepared ionic liquid [AEEAIm][AA] is dissolved in the phase-separating agent n-butanol; specifically, the mass ratio of the [AEEAIm] ionic liquid to n-butanol is 2:1, and the two components account for 60% of the total absorbent. Then, an accelerator, MEA, is added to the system, accounting for 10% of the total absorbent system. The remaining component is a certain amount of water. Finally, after mixing and stirring, a phase change absorbent can be prepared, labeled as H-1.

[0063] Example 2:

[0064] First, a certain amount of the prepared ionic liquid [AEEAIm][AA] is dissolved in the phase-separating agent n-butanol; specifically, the mass ratio of the [AEEAIm] ionic liquid to n-butanol is 2:1, and the two components account for 65% of the entire absorbent. Then, an accelerator, MEA, is added to the above system, accounting for 10% of the entire absorption system. The remaining component is a certain amount of water. Finally, after mixing and stirring, a phase change absorbent can be prepared, which is labeled as H-2.

[0065] Example 3:

[0066] First, a certain amount of the prepared ionic liquid [AEEAIm][AA] is dissolved in the phase-separating agent n-butanol; specifically, the mass ratio of the [AEEAIm] ionic liquid to n-butanol is 2:1, and the two components account for 60% of the entire absorbent. Then, an accelerator, MEA, is added to the above system, accounting for 15% of the entire absorption system. The remaining component is a certain amount of water. Finally, after mixing and stirring, a phase change absorbent can be prepared, which is labeled as H-3.

[0067] Example 4:

[0068] First, a certain amount of the prepared ionic liquid [AEEAIm][AA] is dissolved in the phase-separating agent n-butanol; specifically, the mass ratio of the [AEEAIm] ionic liquid to n-butanol is 2:1, and the two components account for 65% of the entire absorbent. Then, an accelerator, MEA, is added to the above system, accounting for 15% of the entire absorption system. The remaining component is a certain amount of water. Finally, after mixing and stirring, a phase change absorbent can be prepared, which is labeled as H-4.

[0069] The table below shows the absorption and desorption performance test results of the phase change absorbent and MEA absorbent of this application;

[0070]

[0071] In summary, the table above shows that compared with MEA, phase change CO2 absorbents have improved absorption capacity and circulation capacity, as well as increased desorption efficiency; therefore, their carbon capture performance is superior to that of commercial absorbent MEA.

[0072] The above description is merely an embodiment of the present invention and does not limit the patent scope of the present invention. Any equivalent structural or procedural transformations made based on the content of the present invention's specification and drawings, or direct or indirect applications in other related technical fields, are similarly included within the patent protection scope of the present invention.

Claims

1. An application system for a carbon dioxide absorbent, characterized in that: It includes a carbon capture performance testing device, which includes a laboratory absorption-desorption device and an industrial pilot-scale device; The industrial pilot-scale device includes an absorption tower (1), which is connected to an absorbent storage structure and a raw material gas storage structure. The gas output end of the top of the absorption tower (1) is connected to a first gas-liquid separator (2), the gas output end of the first gas-liquid separator (2) is connected to a first gas analyzer (3), and the liquid output end of the first gas-liquid separator (2) is connected to the liquid input end of the absorption tower (1). The liquid output end at the bottom of the absorption tower (1) is connected to a two-phase separator (4). The upper output end of the two-phase separator (4) is connected to the gas input end at the top of the absorption tower (1) through a first conveying mechanism. The lower output end of the two-phase separator (4) is connected to a lean and rich liquid heat exchanger (5) through a second conveying mechanism. The liquid output end of the lean and rich liquid heat exchanger (5) is connected to a desorption tower (6), the desorption tower (6) is connected to a reboiler (7), the gas output end of the desorption tower (6) is connected to a second gas-liquid separator (8), the gas output end of the second gas-liquid separator (8) is connected to a second gas analyzer (9), and the liquid output end of the second gas-liquid separator (8) is connected to the liquid input end of the desorption tower (6). The liquid output end of the reboiler (7) is connected to the liquid input end of the lean-rich liquid heat exchanger (5) through a third conveying mechanism, and the liquid output end of the lean-rich liquid heat exchanger (5) is connected to the liquid input end at the top of the absorption tower (1) through a fourth conveying mechanism.

2. The carbon dioxide absorbent application system according to claim 1, characterized in that: The first conveying mechanism includes a first conveying pipe (13) connected between the two-phase separator (4) and the absorption tower (1), and a lean phase pump (14) is provided on the first conveying pipe (13).

3. The carbon dioxide absorbent application system according to claim 1, characterized in that: The second conveying mechanism includes a second conveying pipe (15) connected between the two-phase separator (4) and the lean and rich liquid heat exchanger (5), and a rich liquid pump (16) is provided on the second conveying pipe (15).

4. The carbon dioxide absorbent application system according to claim 1, characterized in that: The third conveying mechanism includes a third conveying pipe (18) connected between the reboiler (7) and the lean and rich liquid heat exchanger (5), and a lean liquid pump (19) is provided on the third conveying pipe (18).

5. The carbon dioxide absorbent application system according to claim 1, characterized in that: A first cooler (17) is connected between the gas output end of the desorption tower (6) and the gas input end of the second gas-liquid separator (8).

6. The application system of a carbon dioxide absorbent according to claim 1, characterized in that: The fourth conveying mechanism includes a fourth conveying pipe (20) connected between the lean and rich liquid heat exchanger (5) and the absorption tower (1), and a lean liquid cooling pump (21) and a second cooler (22) are sequentially arranged on the fourth conveying pipe (20).

7. The carbon dioxide absorbent application system according to claim 1, characterized in that: A flow meter (12) is connected between the first gas-liquid separator (2) and the first gas analyzer (3) and between the second gas-liquid separator (8) and the second gas analyzer (9).

8. The application system of a carbon dioxide absorbent according to claim 1, characterized in that: The two-phase separator (4) has a cone-shaped structure that is wider at the top and narrower at the bottom, and the material of the two-phase separator (4) is transparent organic glass.

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