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CN-224221075-U - Application system of carbon dioxide absorbent

CN224221075UCN 224221075 UCN224221075 UCN 224221075UCN-224221075-U

Abstract

The application discloses an application system of a carbon dioxide absorbent, which relates to the technical field of absorbent, and can be prepared into a novel phase-change type CO 2 absorbent by mixing ionic liquid hydroxyethyl ethylenediamine imidazole-amino acid serving as a main absorbent, ethanolamine/piperazine serving as an accelerant, n-butanol serving as a phase-splitting agent and a certain amount of water, so that the absorption capacity is high, the absorption efficiency is ensured, the regeneration energy consumption is greatly reduced, the stability is good, meanwhile, a carbon capture performance testing device is designed to be a movable skid-mounted type, and a two-phase separator with a wide whole and a narrow whole is utilized, so that the phase separation can be realized quickly, the connection with industrial production side lines is easy, and the industrial performance verification of the absorbent can be further realized quickly.

Inventors

  • HUO MIAOMIAO
  • LI ZHIYI
  • LU ZHENYU
  • YAO QIANG
  • HUANG CHICHENG

Assignees

  • 瀚蓝环境股份有限公司
  • 瀚蓝(佛山)新能源运营有限公司

Dates

Publication Date
20260512
Application Date
20250516

Claims (8)

  1. 1. The application system of the carbon dioxide absorbent is characterized by comprising a carbon capture performance testing device, wherein the carbon capture performance testing device comprises a laboratory absorption-desorption device and an industrial test bench device; The industrial test small-scale device comprises an absorption tower (1), wherein the absorption tower (1) is respectively connected with an absorbent storage structure and a raw gas storage structure, a gas output end at the top of the absorption tower (1) is connected with a first gas-liquid separator (2), a gas output end of the first gas-liquid separator (2) is connected with a first gas analyzer (3), and a liquid output end of the first gas-liquid separator (2) is connected with a liquid input end of the absorption tower (1); The liquid output end at the bottom of the absorption tower (1) is connected with a two-phase separator (4), the upper layer output end of the two-phase separator (4) is connected with the gas input end at the top of the absorption tower (1) through a first conveying mechanism, and the lower layer output end of the two-phase separator (4) is connected with a lean-rich liquid heat exchanger (5) through a second conveying mechanism; The liquid output end of the lean-rich liquid heat exchanger (5) is connected with a desorption tower (6), the desorption tower (6) is connected with a reboiler (7), the gas output end of the desorption tower (6) is connected with a second gas-liquid separator (8), the gas output end of the second gas-liquid separator (8) is connected with a second gas analyzer (9), and the liquid output end of the second gas-liquid separator (8) is connected with the liquid input end of the desorption tower (6); The liquid output end of the reboiler (7) is connected with 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 with the liquid input end at the top of the absorption tower (1) through a fourth conveying mechanism.
  2. 2. A carbon dioxide absorbent application system according to claim 1, wherein the first conveying means comprises a first conveying pipe (13) connected between the two-phase separator (4) and the absorption tower (1), respectively, and a lean phase pump (14) is arranged on the first conveying pipe (13).
  3. 3. A carbon dioxide absorbent application system according to claim 1, wherein the second conveying means comprises a second conveying pipe (15) connected between the two-phase separator (4) and the lean-rich liquid heat exchanger (5), respectively, and a rich liquid pump (16) is arranged on the second conveying pipe (15).
  4. 4. A carbon dioxide absorbent application system according to claim 1, wherein the third conveying means comprises a third conveying pipe (18) connected between the reboiler (7) and the lean-rich liquid heat exchanger (5), respectively, and a lean liquid pump (19) is arranged on the third conveying pipe (18).
  5. 5. The system for carbon dioxide absorbent according to claim 1, characterized in that a first cooler (17) is connected between the gas output of the desorber (6) and the gas input of the second gas-liquid separator (8).
  6. 6. The application system of the carbon dioxide absorbent according to claim 1, wherein the fourth conveying mechanism comprises a fourth conveying pipeline (20) connected between the lean-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 pipeline (20).
  7. 7. The application system of the carbon dioxide absorbent according to claim 1, wherein a flowmeter (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. 8. The application system of the carbon dioxide absorbent according to claim 1, wherein the two-phase separator (4) is of a conical structure with a wide upper part and a narrow lower part, and the two-phase separator (4) is made of transparent organic glass.

Description

Application system of carbon dioxide absorbent Technical Field The application relates to the technical field of absorbents, in particular to an application system of a carbon dioxide absorbent. Background The CO 2 capture technology currently used on a large scale in industry is the alcohol amine solution absorption process, the most common commercial absorbent being monoethanolamine. Monoethanolamine (MEA) has high absorption capacity and good selectivity, but has high regeneration energy consumption, and the amine group is easy to thermally degrade and oxidatively degrade in the heating process. Studies have shown that the water content in MEA solutions can be reduced from 70% to 60% and the regeneration energy consumption can be reduced from 3.29GJ to 3.01GJ/tCO 2. Excessive regeneration energy consumption will greatly increase the operating cost of the CO 2 capture technology, thereby limiting its industrial application. Compared with the traditional amine solution absorbent, the ionic liquid material has the advantages of low regeneration energy consumption, good water resistance, low corrosiveness and the like, and has wide application prospect in the adsorption field. However, ionic liquids also suffer from high viscosity of the rich phase, difficult regeneration, and the like. The liquid-liquid phase change solvent has wide development prospect in the aspect of reducing regeneration energy consumption. The liquid-liquid phase change absorbent can reduce the volume of regenerated rich phase, can greatly reduce the energy consumption of carbon capture after being coupled with an energy-saving process, and the related research becomes a key focus direction for developing a novel carbon capture technology. The method can reduce the viscosity of the ionic liquid absorbent, combines the advantages of the phase change absorbent, ensures the absorption efficiency, can greatly reduce the regeneration energy consumption, and is the research and development direction of the current absorbent. Therefore, in order to solve the above-mentioned problems, it is desirable to provide a novel application of the phase-change CO 2 absorbent. Disclosure of utility model The application aims to provide an application system of a carbon dioxide absorbent, which aims to solve the problems of high viscosity, difficult regeneration and poor stability of the conventional ionic liquid absorbent. The application provides an application system of a carbon dioxide absorbent, which adopts the following technical scheme: An application system of a carbon dioxide absorbent, wherein the carbon dioxide absorbent is applied to the performance test of the absorbent through a carbon capture performance test device, and the carbon capture performance test device comprises a laboratory absorption-desorption device and an industrial test bench device; The industrial test small-scale device comprises an absorption tower, wherein the absorption tower is respectively connected with an absorbent storage structure and a raw gas storage structure, a gas output end at the top of the absorption tower is connected with a first gas-liquid separator, a gas output end of the first gas-liquid separator is connected with a first gas analyzer, and a liquid output end of the first gas-liquid separator is connected with a liquid input end of the absorption tower; The liquid output end at the bottom of the absorption tower is connected with a two-phase separator, the upper layer output end of the two-phase separator is connected with the gas input end at the top of the absorption tower through a first conveying mechanism, and the lower layer output end of the two-phase separator is connected with a lean-rich liquid heat exchanger through a second conveying mechanism; The liquid output end of the lean-rich liquid heat exchanger is connected with a desorption tower, the desorption tower is connected with a reboiler, the gas output end of the desorption tower is connected with a second gas-liquid separator, the gas output end of the second gas-liquid separator is connected with a second gas analyzer, and the liquid output end of the second gas-liquid separator is connected with the liquid input end of the desorption tower; The liquid output end of the reboiler is connected with the liquid input end of the lean-rich liquid heat exchanger through a third conveying mechanism, and the liquid output end of the lean-rich liquid heat exchanger is connected with the liquid input end at the top of the absorption tower through a fourth conveying mechanism. Further, the first conveying mechanism comprises a first conveying pipeline which is respectively connected between the two-phase separator and the absorption tower, and a lean phase pump is arranged on the first conveying pipeline. Further, the second conveying mechanism comprises second conveying pipelines which are respectively connected between the two-phase separator and the lean-rich liquid heat exchanger, and a