An adjustable, intensified, regenerative organic amine process carbon capture system

Abstract

The application discloses a kind of adjustable, reinforced regenerative organic amine method carbon capture system, belong to carbon dioxide capture technical field, including regeneration reactor, regeneration reactor is sequentially divided into gas-liquid separation zone, desorption reaction zone and reinforced desorption zone from top to bottom, gas-liquid separation zone is communicated with lean-rich liquid heat exchanger, desorption reaction zone is communicated with preheater, lean-rich liquid heat exchanger is communicated with preheater, the top of gas-liquid separation zone is communicated with gas-liquid separator, and liquid collecting pan is arranged between desorption reaction zone and reinforced desorption zone, liquid collecting pan is communicated with reboiler, and lean-rich liquid heat exchanger is communicated with preheater.The application can control the reasonable distribution gradient that regeneration reactor internal radial temperature is at, strengthens desorption efficiency, controls the temperature of regeneration reactor outlet simultaneously, reduces the heat loss that regeneration gas carries out, reduces desorption energy consumption.

Description

Technical Field

[0001] This invention belongs to the field of carbon dioxide capture technology, and particularly relates to an adjustable and enhanced regeneration organic amine carbon capture system. Background Technology

[0002] The efficient capture and resource utilization of carbon dioxide in industrial flue gas has become a key technological pathway for reducing carbon emissions. Organic amine methods, due to their high absorption efficiency and selectivity, have become one of the mainstream technologies in the current carbon capture field. Organic amine carbon dioxide capture mainly includes the absorption and desorption processes. The absorption process involves contacting CO2 with a chemical absorbent, absorbing CO2 into the organic amine solution. The desorption process involves desorbing the CO2-saturated organic amine solution to regenerate the solution. An efficient desorption process requires two key conditions to be met simultaneously: first, a suitable desorption temperature range (100~110℃) to promote the forward desorption reaction of CO2; and second, sufficient effective desorption time to ensure complete dissociation of CO2 from the organic amine solution.

[0003] In existing organic amine carbon dioxide capture systems, the desorption reaction of the solution generally occurs in a packed regeneration tower, using a siphon reboiler or falling film reboiler to heat the solution at the bottom of the tower. This structure has two main drawbacks during the desorption process: Firstly, the rich amine solution discharged from the absorption tower, after being preheated by a lean amine heat exchanger, is difficult to reach the temperature threshold required for the desorption reaction in the highly dispersed contact area of ​​the packed section of the regeneration tower due to factors such as heat exchanger efficiency and heat loss along the pipeline. The temperature distribution within the regeneration tower is not adjustable, resulting in low gas-liquid mass and heat transfer efficiency. Secondly, the solution in the regeneration tower bottom is heated to the desorption temperature by the reboiler, and the solution in the bottom is in a static or low-flow-rate state, resulting in low internal heat transfer efficiency and limiting the desorption efficiency. Therefore, developing a carbon capture device and system that can dynamically adjust according to operating conditions, enhance regeneration effects, and reduce energy consumption has become a key requirement for the development of organic amine carbon capture technology. Summary of the Invention

[0004] The purpose of this invention is to provide an adjustable and enhanced regeneration organic amine carbon capture system to solve the problems existing in the prior art.

[0005] To achieve the above objectives, the present invention provides the following solution: The present invention provides an adjustable and enhanced regeneration organic amine carbon capture system, comprising a regeneration reactor, wherein the regeneration reactor is divided into a gas-liquid separation zone, a desorption reaction zone, and an enhanced desorption zone from top to bottom. The gas-liquid separation zone is connected to a lean-rich liquid heat exchanger, the desorption reaction zone is connected to a preheater, the lean-rich liquid heat exchanger is connected to the preheater, a gas-liquid separator is connected to the top of the gas-liquid separation zone, a liquid collection plate is provided between the desorption reaction zone and the enhanced desorption zone, the liquid collection plate is connected to a reboiler, and the enhanced desorption zone is connected to the lean-rich liquid heat exchanger.

[0006] Optionally, the gas-liquid separation zone is provided with a first rich liquid inlet, which is connected to the lean-rich liquid heat exchanger.

[0007] Optionally, the desorption reaction zone is provided with a second rich liquid inlet, which is connected to the lean and rich liquid heat exchanger through the preheater.

[0008] Optionally, the reboiler is provided with a reboiler solution inlet and a reboiler solution outlet, and the liquid collection tray is provided with a first lean liquid outlet, which is connected to the reboiler solution inlet, and the reboiler solution outlet is connected to the solution inlet of the enhanced desorption zone.

[0009] Optionally, the enhanced desorption zone is provided with a second lean liquid outlet, which is connected to a lean liquid pump, and the lean liquid pump is connected to the lean-rich liquid heat exchanger.

[0010] Optionally, the regeneration reactor is provided with a regeneration gas outlet at the top, the regeneration gas outlet is connected to a regeneration gas cooler, and the regeneration gas cooler is connected to the gas-liquid separator.

[0011] Optionally, the gas-liquid separation zone is equipped with metal packing material.

[0012] Optionally, the desorption reaction zone is provided with metal packing or packing catalyst.

[0013] Optionally, the ratio of the liquid enrichment in the gas-liquid separation zone to the liquid enrichment in the desorption reaction zone can be adjusted to a range of 1:9 to 5:5.

[0014] Optionally, the internal pressure of the regeneration reactor is 20 kPa to 90 kPa.

[0015] The present invention discloses the following technical effects: The present invention can control the radial temperature inside the regeneration reactor to be in a reasonable distribution gradient, thereby enhancing the desorption efficiency. At the same time, it controls the temperature at the outlet of the regeneration reactor, reduces the heat loss carried out by the regeneration gas, and reduces the desorption energy consumption. Attached Figure Description

[0016] The accompanying drawings, which form part of this application, are used to provide a further understanding of this application. The embodiments of this application and their descriptions are used to explain this application and do not constitute an undue limitation of this application. In the drawings: Figure 1 This is a schematic diagram of the adjustable and enhanced regeneration organic amine carbon capture system of the present invention.

[0017] Figure label: 1. Regeneration reactor; 101. Gas-liquid separation zone; 102. Desorption reaction zone; 103. Enhanced desorption zone; 2. Lean and rich liquid heat exchanger; 3. Gas-liquid separator; 4. Liquid collection tray; 5. Reboiler; 6. First rich liquid inlet; 7. Second rich liquid inlet; 8. Preheater; 9. First lean liquid outlet; 10. Second lean liquid outlet; 11. Lean liquid pump; 12. Regeneration gas outlet; 13. Regeneration gas cooler. Detailed Implementation

[0018] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0019] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0020] Reference Figure 1 As shown, this embodiment provides an adjustable and enhanced regeneration organic amine carbon capture system, including a regeneration reactor 1. The regeneration reactor 1 is divided into a gas-liquid separation zone 101, a desorption reaction zone 102, and an enhanced desorption zone 103 from top to bottom. The gas-liquid separation zone 101 is connected to a lean-rich liquid heat exchanger 2. The desorption reaction zone 102 is connected to a preheater 8. The lean-rich liquid heat exchanger 2 is connected to the preheater 8. The top of the gas-liquid separation zone 101 is connected to a gas-liquid separator 3. A liquid collection plate 4 is provided between the desorption reaction zone and the enhanced desorption zone 103. The liquid collection plate 4 is connected to a reboiler 5. The enhanced desorption zone 103 is connected to the lean-rich liquid heat exchanger 2.

[0021] The desorption reaction zone 102 and the enhanced desorption zone 103 are separated by the liquid collection plate 4, forming two relatively independent regions. Gas in the enhanced desorption zone 103 can rise to the desorption reaction zone 102 through the gas riser of the liquid collection plate 4, but the liquid in the desorption reaction zone 102 is intercepted by the liquid collection plate 4 and cannot directly enter the enhanced desorption zone 103.

[0022] The present invention can control the radial temperature inside the regeneration reactor 1 to be in a reasonable distribution gradient, thereby enhancing the desorption efficiency. At the same time, it can control the temperature at the outlet of the regeneration reactor 1, reduce the heat loss carried out by the regeneration gas, and reduce the desorption energy consumption.

[0023] The scheme is further optimized by providing a first rich liquid inlet 6 in the gas-liquid separation zone 101, which is connected to the lean and rich liquid heat exchanger 2.

[0024] The scheme is further optimized by providing a second rich liquid inlet 7 in the desorption reaction zone 102, which is connected to the lean and rich liquid heat exchanger 2 through the preheater 8.

[0025] After being heated, the rich liquor is divided into two streams. One stream directly enters the gas-liquid separation zone 101 of the regeneration reactor 1, while the other stream enters the preheater 8 and is heated to 95℃~110℃ before entering the desorption reaction zone 102 of the regeneration reactor 1. In the desorption reaction zone 102, the rich liquor undergoes sufficient heat exchange with the gas rising from the bottom of the regeneration reactor 1 and undergoes a desorption reaction in the packing or the packing catalytic section to release carbon dioxide and obtain the first lean liquor.

[0026] The scheme is further optimized. The reboiler 5 is provided with a solution inlet and a solution outlet. The liquid collection tray 4 is provided with a first lean liquid outlet 9, which is connected to the solution inlet of the reboiler 5. The solution outlet of the reboiler 5 is connected to the solution inlet of the enhanced desorption zone 103.

[0027] The first lean liquor accumulates on the upper part of the collection plate 4 in the regeneration reactor 1, and enters the reboiler 5 to be heated again to 100℃~120℃. The heated lean liquor is returned to the enhanced desorption zone 103 at the bottom of the regeneration reactor 1 for further desorption to ensure the full removal of carbon dioxide and obtain the second lean liquor.

[0028] The scheme has been further optimized, and the desorption zone 103 is equipped with a second lean liquid outlet 10. The second lean liquid outlet 10 is connected to a lean liquid pump 11, which is connected to a lean and rich liquid heat exchanger 2.

[0029] In a further optimized design, the top of the regeneration reactor 1 is provided with a regeneration gas outlet 12, which is connected to a regeneration gas cooler 13, and the regeneration gas cooler 13 is connected to a gas-liquid separator 3.

[0030] The dehydrated regenerated gas is discharged from the top outlet of the regeneration reactor 1. The regenerated gas is cooled to below 50°C by the regenerated gas cooler 13 and then enters the gas-liquid separator 3 to separate the condensate from the regenerated gas. The condensate is returned to the system. The carbon dioxide enters the subsequent purification, compression or storage unit.

[0031] The design has been further optimized by incorporating metal packing material into the gas-liquid separation zone 101 to enhance gas-liquid separation efficiency.

[0032] To further optimize the design, the desorption reaction zone 102 is equipped with metal packing material or packing catalyst. The packing catalyst can be a molecular sieve catalyst, an alumina catalyst, a solid acid metal oxide catalyst, or similar type.

[0033] To further optimize the scheme, the heat source for preheater 8 can be selected from the steam condensate of reboiler 5, externally supplied steam, or a combination of the two heat sources.

[0034] An adjustable and enhanced regeneration method for organic amine-based carbon capture includes the following steps: S1. The rich liquid from the absorption tower, which has absorbed carbon dioxide, first enters the lean-rich liquid heat exchanger 2 to exchange heat with the lean liquid, completing the initial temperature rise. The heated rich liquid is divided into two paths. One path directly enters the gas-liquid separation zone 101 of the regeneration reactor 1, and the other path enters the preheater 8 to be heated to 95℃~110℃ before entering the desorption reaction zone 102 of the regeneration reactor 1. In the desorption reaction zone 102, the rich liquid in this path undergoes sufficient heat exchange with the gas rising from the bottom of the regeneration reactor 1 and undergoes a desorption reaction in the packing or the packing catalytic section to release carbon dioxide, thus obtaining the first lean liquid. S2. The carbon dioxide and water vapor mixture desorbed from the rich liquid in the regeneration reactor 1 flows radially upward along the regeneration reactor 1 to the gas-liquid separation zone 101, where it undergoes mass and heat transfer with the rich liquid entering from the upper part of the gas-liquid separation zone 101. The temperature of the mixed gas decreases, and most of the water vapor is condensed into liquid and mixed with the rich liquid, flowing back into the regeneration reactor 1 to participate in subsequent desorption reactions. The dehydrated regeneration gas is discharged from the top outlet of the regeneration reactor 1, and after being cooled to below 50°C by the regeneration gas cooler 13, it enters the gas-liquid separator 3 to separate the condensate from the regeneration gas. The condensate is returned to the system. The carbon dioxide enters the subsequent purification, compression, or storage unit. S3. The first lean liquor accumulates on the upper part of the collection plate 4 in the regeneration reactor 1, and enters the reboiler 5 to be heated again to 100℃~120℃. The heated lean liquor returns to the enhanced desorption zone 103 at the bottom of the regeneration reactor 1 for further desorption to ensure the full removal of carbon dioxide, and obtains the second lean liquor. The second lean liquor is sent to the lean-rich liquor heat exchanger 2 through the lean liquor pump 11 to exchange heat with the rich liquor to be treated to achieve heat recovery. Then, it is cooled to the required operating temperature of the absorption tower by the lean liquor cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0035] Further optimization of the scheme involves dynamically adjusting the distribution ratio of the rich liquid entering the gas-liquid separation zone 101 and the desorption reaction zone 102 of the regeneration reactor 1 based on changes in the carbon dioxide load (i.e., the volume of carbon dioxide per unit volume of rich liquid). The adjustment range is 1:9 to 5:5. When the carbon dioxide load in the rich liquid is high, the amount of rich liquid entering the preheater 8 can be increased to enhance the reaction intensity of the desorption reaction zone 102. When the load is low, the amount of rich liquid directly entering the gas-liquid separation zone 101 can be increased to reduce the heat carried out by the regeneration gas at the outlet of the regeneration reactor 1. Through this adjustment mechanism, the radial temperature inside the regeneration reactor 1 is controlled at a reasonable distribution gradient, enhancing the desorption efficiency. At the same time, the temperature of the regeneration gas exiting the regeneration reactor 1 is controlled to reduce the heat loss carried out by the regeneration gas and reduce desorption energy consumption.

[0036] Further optimization of the scheme involves setting the internal pressure of regeneration reactor 1 to 20 kPa to 90 kPa, thereby reducing the boiling point of the organic amine solution, decreasing the energy consumption required for the desorption process, and ensuring the desorption efficiency of carbon dioxide.

[0037] Taking a coal-fired flue gas capture device with an annual output of 10,000 tons of carbon dioxide organic amine chemical absorption method (35%MEA) as an example, the amine liquid flow rate is set to 21t / h, the rich liquid load is controlled to 60L / L by adjusting the liquid-to-gas ratio, the rich amine liquid and the hot lean liquid exchange heat in the lean-rich liquid heat exchanger 2, and the heat of the hot lean liquid is recovered.

[0038] Example 1 The amine solution flow rate is set to 21 t / h, and the load of the rich solution after absorbing carbon dioxide is 60 L / L. After passing through the lean-rich solution heat exchanger 2, the temperature of the rich solution rises to 90℃. It then enters the preheater 8 and is heated to 110℃. It enters the desorption reaction zone 102 of the regeneration reactor 1 from the second rich solution inlet 7. After desorption, the rich solution yields the first lean solution and carbon dioxide gas. The temperature of the first lean solution decreases, and it enters the reboiler 5 and is heated to 110℃ again. It then enters the enhanced desorption zone 103 of the regeneration reactor 1 for further desorption to obtain the second lean solution and carbon dioxide gas. The second lean solution is sent to the lean-rich solution heat exchanger 2 through the lean solution pump 11 to exchange heat with the rich solution to be treated, thereby realizing heat recovery. Subsequently, it is cooled to the operating temperature required by the absorption tower by the lean solution cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0039] In this Example 1, the temperature of the amine solution had reached the desorption temperature when it entered the desorption reaction zone 102. After efficient desorption, the lean liquid load was 22.1 L / L, the load difference was 37.9 L / L, and the desorption efficiency (load difference / rich liquid load) was 63.2%. The top temperature of the regeneration reactor 1 was 100℃, the steam flow rate consumed by the preheater 8 was 783 kg / h, the steam flow rate consumed by the reboiler 5 was 1776 kg / h, the carbon dioxide production was 1.56 t / h, and the comprehensive energy consumption was 3.60 GJ / tCO2.

[0040] Example 2 The amine solution flow rate is set to 21 t / h, and the load of the rich solution after carbon dioxide absorption is 60 L / L. After passing through the rich-lean-lean heat exchanger 2, the temperature of the rich solution rises to 90℃. 30% enters the gas-liquid separation zone 101 of the regeneration reactor 1 from the first rich solution inlet 6, and 70% enters the preheater 8. The rich solution is heated to 110℃ in the preheater 8 and enters the desorption reaction zone 102 of the regeneration reactor 1 from the second rich solution inlet 7. After desorption, the rich solution yields the first lean solution and carbon dioxide gas. The temperature of the first lean solution decreases and it enters the reboiler 5 to be reheated to 110℃. It then enters the enhanced desorption zone 103 of the regeneration reactor 1 for further desorption to obtain the second lean solution and carbon dioxide gas. The second lean solution is sent to the rich-lean-lean heat exchanger 2 through the lean solution pump 11 to exchange heat with the rich solution to be treated, thereby realizing heat recovery. Subsequently, it is cooled to the required operating temperature of the absorption tower by the lean solution cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0041] In this Example 2, the temperature of the amine solution has reached the desorption temperature when it enters the desorption reaction zone 102, and the heat at the top of the regeneration reactor 1 is recovered, further reducing energy loss. The lean liquid load after efficient desorption is 26.7 L / L, the load difference is 33.3 L / L, and the desorption efficiency is 55.5%. The temperature at the top of the regeneration reactor 1 is 86℃, the latent heat loss of vaporization is reduced, the steam flow rate consumed by the preheater 8 is 548 kg / h, the steam flow rate consumed by the reboiler 5 is 1662 kg / h, the carbon dioxide production is 1.37 t / h, and the comprehensive energy consumption is 3.54 GJ / tCO2.

[0042] Example 3 The amine solution flow rate is set to 21 t / h, and the load of the rich solution after carbon dioxide absorption is 60 L / L. After passing through the lean-rich solution heat exchanger 2, the temperature of the rich solution rises to 90℃. 15% enters the gas-liquid separation zone 101 of the regeneration reactor 1 from the first rich solution inlet 6, and 85% enters the preheater 8. The rich solution is heated to 110℃ in the preheater 8 and enters the desorption reaction zone 102 of the regeneration reactor 1 from the second rich solution inlet 7. After desorption, the rich solution yields the first lean solution and carbon dioxide gas. The temperature of the first lean solution decreases and it enters the reboiler 5 for reheating to 110℃. It then enters the enhanced desorption zone 103 of the regeneration reactor 1 for further desorption to obtain the second lean solution and carbon dioxide gas. The second lean solution is sent to the lean-rich solution heat exchanger 2 through the lean solution pump 11 to exchange heat with the rich solution to be treated, thereby realizing heat recovery. Subsequently, it is cooled to the required operating temperature of the absorption tower by the lean solution cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0043] In this Example 3, the temperature of the amine solution has reached the desorption temperature when it enters the desorption reaction zone 102, and the heat at the top of the regeneration reactor 1 is recovered, further reducing energy loss. The lean liquid load after efficient desorption is 24.5 L / L, the load difference is 35.5 L / L, and the desorption efficiency is 59.2%. The top temperature of the regeneration reactor 1 is 88℃, the steam flow rate consumed by the preheater 8 is 665 kg / h, the steam flow rate consumed by the reboiler 5 is 1671 kg / h, the carbon dioxide production is 1.46 t / h, and the comprehensive energy consumption is 3.51 GJ / tCO2.

[0044] Example 4 The difference from Example 3 is that the desorption reaction zone 102 is equipped with catalyst packing, and the steam condensate from the reboiler 5 is used as the heat source for the preheater 8. The specific implementation process is as follows: The amine solution flow rate is set to 21 t / h, and the load of the rich solution after carbon dioxide absorption is 60 L / L. After passing through the rich-lean-rich solution heat exchanger 2, the temperature of the rich solution rises to 85℃. 15% enters the gas-liquid separation zone 101 of the regeneration reactor 1 from the first rich solution inlet 6, and 85% enters the preheater 8. The rich solution is heated to 95℃ in the preheater 8 and enters the desorption reaction zone 102 of the regeneration reactor 1 from the second rich solution inlet 7. After desorption, the rich solution yields the first lean solution and carbon dioxide gas. The temperature of the first lean solution decreases and it enters the reboiler 5 for reheating to 108℃. It then enters the enhanced desorption zone 103 of the regeneration reactor 1 for further desorption to obtain the second lean solution and carbon dioxide gas. The second lean solution is sent to the rich-lean-rich solution heat exchanger 2 through the lean solution pump 11 to exchange heat with the rich solution to be treated, thereby realizing heat recovery. Subsequently, it is cooled to the operating temperature required by the absorption tower by the lean solution cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0045] In this embodiment 4, the desorption temperature range is reduced under the action of the catalyst, and 15% of the desorption is diverted into the gas-liquid separation zone 101 of the regeneration reactor 1. The heat at the top of the regeneration reactor 1 is recovered, further reducing energy loss. After efficient desorption of the amine liquid, the lean liquid load is 20.3 L / L, the load difference is 39.7 L / L, and the desorption efficiency is 66.2%. The top temperature of the regeneration reactor 1 is 85℃, the steam flow rate consumed by the reboiler 5 is 2025 kg / h, the carbon dioxide production is 1.64 t / h, and the comprehensive energy consumption is 2.72 GJ / tCO2.

[0046] Comparative Example 1 Compared with Example 1, the difference is that the preheater 8 is not installed in the system. After the rich liquid passes through the lean-rich liquid heat exchanger 2, it directly enters the desorption reaction zone 102 of the regeneration reactor 1 from the second rich liquid inlet 7.

[0047] The amine solution flow rate is set to 21 t / h, and the rich solution load after carbon dioxide absorption is 60 L / L. After the rich solution passes through the lean-rich solution heat exchanger 2, the temperature is raised to 90℃ and then directly enters the desorption reaction zone 102. The rich amine solution exchanges heat with the steam generated in the tower bottom in the packing. After reaching 105℃, desorption begins to occur, resulting in the first lean solution. It then enters the reboiler 5 and is reheated to 110℃. It then enters the enhanced desorption zone 103 of the regeneration reactor 1 for further desorption, resulting in the second lean solution and carbon dioxide gas. The second lean solution is sent to the lean-rich solution heat exchanger 2 through the lean solution pump 11 to exchange heat with the rich solution to be treated, thereby realizing heat recovery. Subsequently, it is cooled to the required operating temperature of the absorption tower by the lean solution cooler and re-enters the absorption tower to participate in the carbon dioxide absorption process, completing the closed-loop circulation of the organic amine solution.

[0048] In Comparative Example 1, since the rich amine solution only exchanges heat and does not desorb in the packing material at the top of the regeneration reaction zone, the residence time of the amine solution in the packing material during the desorption process is shortened, thus affecting the lean liquor load. The measured lean liquor load is 32.6 L / L, the load difference is only 27.4 L / L, and the desorption efficiency is 45.7%. The top temperature of the regeneration reactor 1 is 84℃, the steam flow rate consumed by the reboiler 5 is 2045 kg / h, the carbon dioxide production is 1.13 t / h, and the comprehensive energy consumption is 3.98 GJ / tCO2.

[0049] The results of Examples 1-4 and Comparative Example 1 are shown in Table 1.

[0050] Table 1 Results analysis: Table 1 shows a comparison of key operating data of Embodiments 1, 2, 3, and 4 of the present invention with Comparative Example 1 under the same working conditions.

[0051] Comparing Example 1 with Comparative Example 1, the only difference is that Example 1 uses preheater 8. Comparing the data in Table 1, the amine desorption efficiency and energy consumption of Example 1 are better than those of Comparative Example 1.

[0052] Comparing Examples 2 and 3 with Example 1, the only difference is that Examples 2 and 3 use a diversion method to feed into the regeneration reactor 1. Comparing the data in Table 1, Examples 2 and 3 show a decrease in desorption efficiency compared to Example 1. However, since the diversion method reduces the top temperature of the regeneration reactor 1, the latent heat loss of gasification is reduced, thus reducing energy consumption.

[0053] Comparing Example 4 with Example 3, the only difference is that the desorption reaction zone 102 of Example 4 is equipped with catalyst packing and the steam condensate of reboiler 5 is used as the heat source of preheater 8. Comparing the data in Table 1, Example 4 is better than Example 3 in terms of desorption efficiency and energy consumption.

[0054] In the description of this invention, it should be understood that the terms "longitudinal", "lateral", "up", "down", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this invention, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this invention.

[0055] The embodiments described above are merely preferred embodiments of the present invention and are not intended to limit the scope of the present invention. Various modifications and improvements made by those skilled in the art to the technical solutions of the present invention without departing from the spirit of the present invention should fall within the protection scope defined by the claims of the present invention.

Claims

1. An adjustable and enhanced regeneration organic amine carbon capture system, characterized in that: The reactor includes a regeneration reactor (1), which is divided into a gas-liquid separation zone (101), a desorption reaction zone (102), and an enhanced desorption zone (103) from top to bottom. The gas-liquid separation zone (101) is connected to a lean-rich liquid heat exchanger (2), the desorption reaction zone (102) is connected to a preheater (8), the lean-rich liquid heat exchanger (2) is connected to the preheater (8), the top of the gas-liquid separation zone (101) is connected to a gas-liquid separator (3), a liquid collection plate (4) is provided between the desorption reaction zone (102) and the enhanced desorption zone (103), the liquid collection plate (4) is connected to a reboiler (5), and the enhanced desorption zone (103) is connected to the lean-rich liquid heat exchanger (2).

2. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The gas-liquid separation zone (101) is provided with a first rich liquid inlet (6), which is connected to the lean and rich liquid heat exchanger (2).

3. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The desorption reaction zone (102) is provided with a second rich liquid inlet (7), which is connected to the lean and rich liquid heat exchanger (2) through the preheater (8).

4. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The reboiler (5) is provided with a reboiler (5) solution inlet and a reboiler (5) solution outlet. The liquid collection plate (4) is provided with a first lean liquid outlet (9). The first lean liquid outlet (9) is connected to the reboiler (5) solution inlet, and the reboiler (5) solution outlet is connected to the solution inlet of the enhanced desorption zone (103).

5. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The enhanced desorption zone (103) is provided with a second lean liquid outlet (10), and the second lean liquid outlet (10) is connected to a lean liquid pump (11), which is connected to the lean and rich liquid heat exchanger (2).

6. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The regeneration reactor (1) is provided with a regeneration gas outlet (12) at the top, the regeneration gas outlet (12) is connected to a regeneration gas cooler (13), and the regeneration gas cooler (13) is connected to the gas-liquid separator (3).

7. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The gas-liquid separation zone (101) is equipped with metal packing.

8. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The desorption reaction zone (102) is equipped with metal packing or packing catalyst.

9. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The ratio of the liquid enrichment in the gas-liquid separation zone (101) and the desorption reaction zone (102) is adjusted to 1:9 to 5:

5.

10. The adjustable and enhanced regeneration organic amine carbon capture system according to claim 1, characterized in that: The internal pressure of the regeneration reactor (1) is 20 kPa to 90 kPa.

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