Carbon dioxide capture system

Abstract

The present application relates to the technical field of carbon dioxide capture, and particularly relates to a carbon dioxide capture system, the carbon dioxide capture system comprises a regeneration tower, the regeneration tower is provided with a first liquid inlet, a second liquid inlet and a third liquid inlet which are arranged at intervals in the extension direction of the regeneration tower, the second liquid inlet is located between the first liquid inlet and the third liquid inlet in the flow direction of the liquid, the regeneration tower is provided with a tray and a filler layer, the filler layer comprises a first filler layer and at least one second filler layer, the tray is arranged between the first liquid inlet and the second liquid inlet so that the first liquid inlet transports condensed liquid to the tray, the first filler layer is arranged between the second liquid inlet and the third liquid inlet so that the second liquid inlet transports a first absorbent to the first filler layer, and the third liquid inlet is used for transporting a second absorbent with a temperature greater than that of the first absorbent to the second filler layer, the carbon dioxide capture system of the present application can reduce the regeneration energy consumption of the regeneration tower.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of carbon dioxide capture, in particular to a carbon dioxide capture system. BACKGROUND

[0002] In the carbon dioxide capture system, the absorbent absorbs carbon dioxide in the flue gas in the absorption tower to form a rich solution and circulates to the regeneration tower for regeneration. In the regeneration process of the rich solution, the rich solution needs to be heated to a certain temperature before the regeneration reaction can be realized, and the loaded carbon dioxide in the rich solution is released. In the related technology, the rich solution is separated into light phase and heavy phase, and the heavy phase is recycled to the regeneration tower for regeneration. However, heating the heavy phase requires a large amount of heat, resulting in high energy consumption of the regeneration tower. SUMMARY

[0003] The present application aims to at least solve one of the technical problems in the related art. To this end, the embodiments of the present application propose a carbon dioxide capture system which can use the heat of carbon dioxide to heat the absorbent, thereby reducing the regeneration energy consumption of the regeneration tower.

[0004] The carbon dioxide capture system of the embodiments of the present application comprises: a regeneration tower, the regeneration tower has a first liquid inlet, a second liquid inlet and a third liquid inlet, the first liquid inlet, the second liquid inlet and the third liquid inlet are arranged at intervals in the extension direction of the regeneration tower, and in the flow direction of the liquid, the first liquid inlet is located upstream of the second liquid inlet, and the second liquid inlet is located upstream of the third liquid inlet; the regeneration tower is provided with a tray and a filler layer, the filler layer comprises a first filler layer and at least one second filler layer, the first filler layer and the second filler layer are arranged at intervals in the extension direction of the regeneration tower, the tray is arranged between the first liquid inlet and the second liquid inlet, the first liquid inlet is used to deliver a condensed liquid to the tray, the first filler layer is arranged between the second liquid inlet and the third liquid inlet, the second liquid inlet is used to deliver a first absorbent to the first filler layer, so that the first absorbent exchanges heat with the gas between the second liquid inlet and the third liquid inlet, the third liquid inlet is used to deliver a second absorbent to the second filler layer, and the temperature of the second absorbent is greater than that of the first absorbent.

[0005] The carbon dioxide capture system of the embodiment of the present application is provided with a first liquid inlet, a second liquid inlet and a third liquid inlet from top to bottom on the regeneration tower, the condensed liquid is sent to the tray through the first liquid inlet to make the condensed liquid exchange mass and heat with the carbon dioxide between the first liquid inlet and the second liquid inlet, the first absorbent is sent to the first packing layer through the second liquid inlet, so that the first absorbent fully contacts and exchanges heat with the carbon dioxide between the second liquid inlet and the third liquid inlet in the first packing layer to increase the temperature of the first absorbent, the second absorbent is sent to the second packing layer through the third liquid inlet, so that the second absorbent fully contacts and exchanges heat with the carbon dioxide below the third liquid inlet in the second packing layer, the carbon dioxide flows from bottom to top and contacts the second absorbent, the first absorbent and the condensed liquid step by step, the heat of the carbon dioxide is transferred to the second absorbent, the first absorbent and the condensed liquid step by step, the step-by-step utilization of heat is realized, and the regeneration energy consumption of the regeneration tower is reduced.

[0006] In some embodiments, the carbon dioxide capture system further comprises a cooler, the cooler has a first channel and a second channel, one end of the first channel is communicated with the gas outlet end of the regeneration tower, one end of the second channel is adapted to be communicated with the liquid outlet end of the absorption tower, the other end of the second channel is communicated with the third liquid inlet, the gas in the first channel and the liquid in the second channel can exchange heat.

[0007] In some embodiments, the carbon dioxide capture system further comprises a heat exchanger, the heat exchanger is arranged between the cooler and the regeneration tower, the heat exchanger has a third channel and a fourth channel, the third channel has a first input end, a second input end and a first output end, the first input end is communicated with the liquid outlet end of the absorption tower, the second input end is communicated with the other end of the second channel, the first output end is communicated with the third liquid inlet, the fourth channel is adapted to be communicated with a heat source, the liquid in the third channel can exchange heat with the heat source in the fourth channel.

[0008] In some embodiments, the input amount of the first input end is greater than the input amount of the second input end, and the input amount of the second input end is greater than the liquid inlet amount of the second liquid inlet.

[0009] In some embodiments, the liquid inlet amount of the third liquid inlet is Q2, the input amount of the first input end is Q21, and the input amount of the second input end is Q22, Q2=Q21+Q22, Q21=a*Q2, the value of a is 0.6-0.8.

[0010] In some embodiments, the sum of the liquid inlet amounts of the second liquid inlet and the third liquid inlet is Q, the liquid inlet amount of the second liquid inlet is Q1, and Q1 = b1 x Q, Q2 = b2 x Q, wherein the value of b1 is 0.1-0.2, and the value of b2 is 0.8-0.9.

[0011] In some embodiments, the liquid inlet amount of the first liquid inlet is Q0, Q0 = b0 x Q, and the value of b0 is 0.95%-0.1%.

[0012] In some embodiments, the size of the second filler layer in the extension direction of the regeneration tower is greater than the size of the first filler layer in the extension direction of the regeneration tower; and / or, the size of the second filler layer in the radial direction of the regeneration tower is greater than the size of the first filler layer in the radial direction of the regeneration tower.

[0013] In some embodiments, the spacing distance between the bottom and the top of the regeneration tower is H, the spacing distance between the first liquid inlet and the top is H1, the spacing distance between the second liquid inlet and the top is H2, and the spacing distance between the third liquid inlet and the top is H3, and H1 = c1 x H, H2 = c2 x H, H3 = c3 x H, wherein the value of c1 is 0.03-0.06, the value of c2 is 0.1-0.2, and the value of c3 is 0.3-0.4.

[0014] In some embodiments, the size of the first liquid inlet in the extension direction of the regeneration tower is L1, the size of the second liquid inlet in the extension direction of the regeneration tower is L2, and the size of the third liquid inlet in the extension direction of the regeneration tower is L3, and the value of L1 is 80-120 mm, the value of L2 is 300-400 mm, and the value of L3 is 800-1000 mm. BRIEF DESCRIPTION OF DRAWINGS

[0015] Figure 1 is a schematic diagram of a carbon dioxide capture system according to an embodiment of the present application.

[0016] Figure 2 is a schematic diagram of a regeneration tower according to an embodiment of the present application.

[0017] REFERENCE SIGNS:

[0018] regeneration tower 1, first liquid inlet 11, second liquid inlet 12, third liquid inlet 13,

[0019] tray 14, filler layer 15, first filler layer 151, second filler layer 152,

[0020] gas outlet end 16 of the regeneration tower, liquid outlet end 17 of the regeneration tower,

[0021] Cooler 2, first channel 21, inlet end 211 of the first channel, outlet end 212 of the first channel, second channel 22, inlet end 221 of the second channel, outlet end 222 of the second channel.

[0022] Heat exchanger 3, third channel 31, first input terminal 311, second input terminal 312, first output terminal 313, fourth channel 32, inlet terminal 321 of the fourth channel, outlet terminal 322 of the fourth channel.

[0023] Absorption tower 4, liquid outlet 41 of the absorption tower, liquid inlet 42 of the absorption tower.

[0024] Phase splitter 5, phase splitter inlet 51, phase splitter outlet 52. Detailed Implementation

[0025] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0026] The carbon dioxide capture system of this embodiment includes a regeneration tower 1, which has a first inlet 11, a second inlet 12, and a third inlet 13. The first inlet 11, the second inlet 12, and the third inlet 13 are located in the extending direction of the regeneration tower 1 (e.g., ...). Figure 1 The components are arranged at intervals in the vertical direction (as shown), and in the direction of liquid flow, the first inlet 11 is located upstream of the second inlet 12, and the second inlet 12 is located upstream of the third inlet 13. The regeneration tower 1 is provided with a tray 14 and a packing layer 15. The packing layer 15 includes a first packing layer 151 and at least one second packing layer 152. The first packing layer 151 and the second packing layer 152 are arranged at intervals in the extension direction of the regeneration tower 1. The tray 14 is located between the first inlet 11 and the second inlet 12. The first inlet 11 is used to deliver condensate to the tray 14. The first packing layer 151 is located between the second inlet 12 and the third inlet 13. The second inlet 12 is used to deliver a first absorbent to the first packing layer 151, so that the first absorbent exchanges heat with the gas between the second inlet 12 and the third inlet 13. The third inlet 13 is used to deliver a second absorbent to the second packing layer 152, and the temperature of the second absorbent is higher than the temperature of the first absorbent.

[0027] Specifically, such as Figure 1 As shown, the first liquid inlet 11 is located above the second liquid inlet 12, and the second liquid inlet 12 is located above the third liquid inlet 13. In the regeneration tower 1, the liquid flows from top to bottom, the absorbent is heated and regenerated in the regeneration tower 1, and the desorbed high-temperature carbon dioxide flows from bottom to top.

[0028] The tray 14 is arranged above the packing layer 15 and between the first liquid inlet 11 and the second liquid inlet 12, that is, the first liquid inlet 11 is arranged above the tray 14, the first liquid inlet 11 is communicated with the condensed liquid, and the condensed liquid is introduced to the upper part of the tray 14 through the first liquid inlet 11. The tray 14 is provided with a riser, and the side of the tray 14 away from the first liquid inlet 11 is provided with an outlet weir. The first liquid inlet 11 delivers the condensed liquid to the upper part of the tray 14, and the condensed liquid flows transversely through the tray 14 and accumulates on the tray 14, and when the accumulation height exceeds the height of the outlet weir, the condensed liquid overflows the outlet weir and flows downward. When the desorbed carbon dioxide at the lower part of the regenerator 1 moves upward to the tray 14, it flows upward through the riser, and the carbon dioxide flows out of the riser and directly contacts the condensed liquid accumulated on the tray 14 to realize mass transfer and heat transfer. During the contact between the condensed liquid and the carbon dioxide, the condensed liquid can remove part of the absorbent carried by the carbon dioxide on one hand, and reduce the content of the absorbent carried by the carbon dioxide, and on the other hand, the temperature of the carbon dioxide can be reduced, and the temperature of the condensed liquid can be increased.

[0029] The first packing layer 151 is arranged above the second packing layer 152, and the first packing layer 151 is located between the second liquid inlet 12 and the third liquid inlet 13, that is, the second liquid inlet 12 is arranged above the first packing layer 151, so as to facilitate the delivery of the first absorbent to the first packing layer 151 through the second liquid inlet 12. The first absorbent and the carbon dioxide flowing upward in the regenerator 1 are fully contacted in the first packing layer 151, so that the temperature of the carbon dioxide is reduced and the temperature of the first absorbent is increased.

[0030] The third liquid inlet 13 is arranged above the second packing layer 152, and the second absorbent is delivered to the second packing layer 152 through the third liquid inlet 13. The second absorbent and the carbon dioxide flowing upward in the regenerator 1 are fully contacted in the second packing layer 152, so that the temperature of the carbon dioxide is reduced and the temperature of the second absorbent is increased.

[0031] For example, the tray 14 is a bubble cap tray 14.

[0032] For example, the number of the second packing layer 152 can be one or multiple. When the number of the second packing layer 152 is multiple, the multiple second packing layers 152 are arranged in the up-down direction. The arrangement of the multiple second packing layers 152 facilitates the full contact between the second absorbent and the carbon dioxide.

[0033] The regenerated tower 1 of the embodiment of the present application is provided with the first liquid inlet 11, the second liquid inlet 12 and the third liquid inlet 13 from top to bottom in sequence, the condensed liquid is transported to the tray 14 through the first liquid inlet 11, and the condensed liquid exchanges mass and heat with the carbon dioxide between the first liquid inlet 11 and the second liquid inlet 12, the first absorbent is transported to the first filler layer 151 through the second liquid inlet 12, so that the first absorbent fully contacts the carbon dioxide between the second liquid inlet 12 and the third liquid inlet 13 in the first filler layer 151 to exchange heat and increase the temperature of the first absorbent, the second absorbent is transported to the second filler layer 152 through the third liquid inlet 13, so that the second absorbent fully contacts the carbon dioxide below the third liquid inlet 13 in the second filler layer 152 to exchange heat, the carbon dioxide flows from bottom to top and gradually contacts the second absorbent, the first absorbent and the condensed liquid, and the heat of the carbon dioxide is gradually transferred to the second absorbent, the first absorbent and the condensed liquid, so that the heat is gradually utilized, and the regeneration energy consumption of the regenerated tower 1 is reduced.

[0034] Further, since the temperature in the regenerated tower 1 gradually rises from top to bottom, the temperature of the first absorbent is set to be lower than that of the second absorbent in the embodiment, which is convenient for adapting to the temperature at the position of the second liquid inlet 12 in the regenerated tower 1, and is convenient for the first absorbent to utilize the heat of the carbon dioxide between the second liquid inlet 12 and the third liquid inlet 13, and the heated first absorbent exchanges heat with the carbon dioxide in the second filler layer 152, so that the utilization efficiency of the heat of the carbon dioxide is improved.

[0035] For example, the temperature of the carbon dioxide at the lowest position in the regenerated tower 1 is about 130℃ during the flow from bottom to top, the temperature of the carbon dioxide is reduced to about 110℃ after heat exchange with the second absorbent, the temperature of the carbon dioxide is reduced to about 100℃ after heat exchange with the first absorbent, and the temperature of the carbon dioxide is further reduced to about 90℃ after heat exchange with the condensed liquid, the heat of the carbon dioxide is gradually utilized, and the heat exchange efficiency is improved by limiting the liquid inlet amount of the first liquid inlet 11, the second liquid inlet 12 and the third liquid inlet 13 in the embodiment.

[0036] In some embodiments, the carbon dioxide capture system further comprises a cooler 2, the cooler 2 has a first passage 21 and a second passage 22, one end of the first passage 21 is in communication with the gas outlet end 16 of the regenerated tower, one end of the second passage 22 is adapted to be in communication with the liquid outlet end 41 of the absorption tower, the other end of the second passage 22 is in communication with the third liquid inlet 13, and the gas in the first passage 21 and the liquid in the second passage 22 can exchange heat.

[0037] Specifically, as shown in FIG. 2, the carbon dioxide capture system further comprises a cooler 2, the cooler 2 has a first passage 21 and a second passage 22, one end of the first passage 21 is in communication with the gas outlet end 16 of the regenerated tower, one end of the second passage 22 is adapted to be in communication with the liquid outlet end 41 of the absorption tower, the other end of the second passage 22 is in communication with the third liquid inlet 13, and the gas in the first passage 21 and the liquid in the second passage 22 can exchange heat. Figure 1As shown, a gas outlet 16 is provided at the top of the regeneration tower 1 to discharge the desorbed carbon dioxide. The inlet 211 of the first channel of the cooler 2 is connected to the gas outlet 16 of the regeneration tower to transfer the carbon dioxide discharged from the regeneration tower 1 into the first channel 21. The outlet 212 of the first channel is connected to the subsequent gas-liquid separator for further processing. The inlet 221 of the second channel is connected to the liquid outlet 41 of the absorption tower to transfer the absorbent discharged from the absorption tower 4 into the second channel 22. The outlet 222 of the second channel is connected to the third liquid inlet 13 of the regeneration tower 1. The carbon dioxide gas in the first channel 21 and the absorbent in the second channel 22 exchange heat, using the heat of the carbon dioxide discharged from the regeneration tower 1 to heat the absorbent, thereby improving the heat utilization efficiency of the carbon dioxide and further reducing the regeneration energy consumption of the regeneration tower 1.

[0038] In some embodiments, the carbon dioxide capture system further includes a heat exchanger 3, which is disposed between the cooler 2 and the regeneration tower 1. The heat exchanger 3 has a third channel 31 and a fourth channel 32. The third channel 31 has a first input end 311, a second input end 312 and a first output end 313. The first input end 311 is connected to the liquid outlet 41 of the absorption tower, the second input end 312 is connected to the other end of the second channel 22, and the first output end 313 is connected to the third liquid inlet 13. The fourth channel 32 is adapted to be circulated with a heat source, and the liquid in the third channel 31 can exchange heat with the heat source in the fourth channel 32.

[0039] Specifically, such as Figure 1 As shown, the upper end of the absorption tower 4 is provided with the liquid inlet 42, and the lower end of the absorption tower 4 is provided with the liquid outlet 41. The second input end 312 of the third channel 31 is connected to the outlet end 222 of the second channel. The lower end of the regeneration tower 1 is provided with the liquid outlet 17 of the regeneration tower. The inlet end 321 of the fourth channel is connected to the liquid outlet end 17 of the regeneration tower to transport the absorbent discharged from the regeneration tower 1 into the fourth channel 32. The outlet end 322 of the fourth channel is connected to the liquid inlet 42 of the absorption tower. The absorbent in the third channel 31 and the absorbent in the fourth channel 32 exchange heat to increase the temperature of the absorbent in the third channel 31 and transport it to the third liquid inlet 13 of the regeneration tower 1.

[0040] Optionally, the absorbent received by the heat exchanger 3 has two paths: the first path is delivered from the liquid outlet 41 of the absorption tower to the heat exchanger 3, and the second path is delivered from the outlet 222 of the second channel of the cooler 2 to the heat exchanger 3. The absorbent in the first and second paths is mixed and then exchanges heat with the heat source in the fourth channel 32 in the heat exchanger 3.

[0041] For example, the carbon dioxide capture system further comprises a phase separator 5, an inlet end 51 of the phase separator is communicated with the liquid outlet end 41 of the absorption tower, a rich phase outlet end 52 of the phase separator is communicated with the second liquid inlet 12, the inlet end 221 of the second passage of the cooler 2 and the first input end 311 of the heat exchanger 3 respectively, the absorbent of the liquid outlet end 41 of the absorption tower is separated by the phase separator 5, and the flow of the absorbent participating in the regeneration is reduced.

[0042] In the embodiment, the temperature of the carbon dioxide discharged from the gas outlet end 16 of the regeneration tower is lower than the temperature of the absorbent discharged from the liquid outlet end 17 of the regeneration tower, a part of the absorbent output from the liquid outlet end 41 of the absorption tower is first introduced into the cooler 2 to be preliminarily heated by the heat in the carbon dioxide discharged from the regeneration tower 1, and then introduced into the heat exchanger 3 to be secondarily heated by the heat in the absorbent discharged from the regeneration tower 1, so that the gradient utilization of the heat is realized, the utilization efficiency of the heat is improved, and the regeneration energy consumption of the regeneration tower 1 is reduced.

[0043] In some embodiments, the input amount of the first input end 311 is greater than the input amount of the second input end 312, and the input amount of the second input end 312 is greater than the liquid inlet amount of the second liquid inlet 12.

[0044] Specifically, as shown in Figure 1 the absorbent output from the liquid outlet end 41 of the absorption tower is divided into three paths, the first path is that the liquid outlet end 41 of the absorption tower is transported to the heat exchanger 3, the second path is that the liquid outlet end 41 of the absorption tower is transported to the cooler 2 and then transported to the heat exchanger 3 after passing through the cooler 2, and the third path is that the liquid outlet end 41 of the absorption tower is transported to the second liquid inlet 12, the flow of the first path is greater than the flow of the second path, and the flow of the second path is greater than the flow of the third path.

[0045] In the embodiment, the input amount of the first input end 311 is set to be greater than the input amount of the second input end 312, that is, the flow of the absorbent in the first path is greater than the flow of the absorbent in the second path, so that the flow of the absorbent in the first path is matched with the flow of the carbon dioxide discharged from the regeneration tower 1, the contact area and the contact time between the absorbent and the carbon dioxide are relatively uniform, and the heat exchange efficiency is improved.

[0046] In the embodiment, the first absorbent is transported through the second liquid inlet 12, so that the first absorbent is heat-exchanged with the carbon dioxide to heat the first absorbent, since the first absorbent is not heated by the cooler 2 and the heat exchanger 3, the temperature of the first absorbent is relatively low, and therefore the flow of the first absorbent is less than the flow of the second absorbent, so that the carbon dioxide is heat-exchanged with the first absorbent to increase the temperature of the first absorbent.

[0047] In some embodiments, the third liquid inlet 13 has a liquid input of Q2, the first input end 311 has an input of Q21, and the second input end 312 has an input of Q22, and Q2=Q21+Q22, Q21=a*Q2, and a is 0.6-0.8.

[0048] In the embodiment, the inputs of the first input end 311 and the second input end 312 are limited, so that the flow rate of the absorbent in the second channel 22 matches the flow rate of the carbon dioxide in the first channel 21. In the case of flow rate matching, the contact area and contact time of the absorbent and the carbon dioxide are relatively uniform, and the heat exchange efficiency is improved.

[0049] For example, a is 0.6, 0.61, 0.65, 0.68, 0.7, 0.73, 0.78, or 0.8. In the embodiment, the specific value of a is not limited, and the flow rate of the absorbent in the second path can be determined according to the flow rate of the carbon dioxide discharged from the regeneration tower 1.

[0050] In some embodiments, the sum of the liquid inputs of the second liquid inlet 12 and the third liquid inlet 13 is Q, the liquid input of the second liquid inlet 12 is Q1, Q1=b1*Q, and Q2=b2*Q, where b1 is 0.1-0.2, and b2 is 0.8-0.9.

[0051] In the embodiment, the liquid inputs of the second liquid inlet 12 and the third liquid inlet 13 are limited, so that the flow rate of the first absorbent delivered by the second liquid inlet 12 into the first filler layer 151 matches the flow rate of the carbon dioxide between the second liquid inlet 12 and the third liquid inlet 13, facilitating heat exchange between the first absorbent and the carbon dioxide and improving the heat exchange efficiency.

[0052] Alternatively, the flow rate of the first absorbent can meet the use of fillers, and the first filler layer 151 can be provided to enable the first absorbent to fully contact the carbon dioxide in the first filler layer 151, improve the mass transfer and heat transfer effect, and reduce the pressure drop in the regeneration tower 1, avoiding the influence of the small pressure in the regeneration tower 1 on the regeneration of the absorbent.

[0053] Further, the flow rate of the first absorbent is relatively small, and the carbon dioxide heats the small-flow first absorbent, on one hand, the heat of the carbon dioxide is used to heat the first absorbent, and on the other hand, the temperature difference between the first absorbent and the carbon dioxide is large, and the heat transfer effect is better.

[0054] For example, b1 is 0.1, 0.11, 0.13, 0.15, 0.155, 0.18, 0.19, or 0.2, and correspondingly, b2 is 0.9, 0.89, 0.87, 0.85, 0.845, 0.82, 0.81, or 0.8.

[0055] For example, the sum of the inlet flow rates of the second inlet 12 and the third inlet 13 is 4100 t / h, of which the inlet flow rate of the second inlet 12 is 600 t / h and the inlet temperature is 40℃, and the inlet flow rate of the third inlet 13 is 3500 t / h and the inlet temperature is 98℃.

[0056] In some embodiments, the liquid inlet volume of the first liquid inlet 11 is Q0, where Q0 = b0 × Q, and the value of b0 is 0.95%-0.1%.

[0057] In this embodiment, the first inlet 11 delivers condensate to the tray 14. The condensate comes into contact with the carbon dioxide gas to lower the temperature of the carbon dioxide and remove the absorbent content carried in the carbon dioxide. By setting the condensate flow rate to a low level, the water content in the absorbent is avoided from being too high.

[0058] Alternatively, since the flow rate of the condensate is relatively small, the form of tray 14 can allow for more thorough gas-liquid contact.

[0059] For example, the value of b0 can be 0.95%, 0.96%, 0.97%, 0.98%, 0.99%, or 0.1%.

[0060] For example, the inlet flow rate of the first inlet 11 is 40t / h, and the inlet temperature is 40℃.

[0061] In some embodiments, the dimension of the second packing layer 152 in the extension direction of the regeneration tower 1 is greater than the dimension of the first packing layer 151 in the extension direction of the regeneration tower 1; and / or, the dimension of the second packing layer 152 in the radial direction of the regeneration tower 1 is greater than the dimension of the first packing layer 151 in the radial direction of the regeneration tower 1.

[0062] Specifically, such as Figure 1 As shown, since the flow rate of the second absorbent is greater than that of the first absorbent, by limiting the height and radial dimensions of the first and second packing layers 151 to accommodate different flow rate settings of the first and second absorbents, the heat exchange efficiency is improved. This is achieved by increasing the height of the second packing layer 152 to be greater than the height of the first packing layer 151, and / or by setting the radial dimension of the second packing layer 152 to be greater than that of the first packing layer 151.

[0063] For example, the second packing layer 152 may have two, three, or four layers.

[0064] In some embodiments, the interval distance between the bottom and the top of the regeneration tower 1 is H, the interval distance between the first liquid inlet 11 and the top is H1, the interval distance between the second liquid inlet 12 and the top is H2, and the interval distance between the third liquid inlet 13 and the top is H3, then H1=c1*H, H2=c2*H, and H3=c3*H, wherein the value of c1 is 0.03-0.06, the value of c2 is 0.1-0.2, and the value of c3 is 0.3-0.4.

[0065] Specifically, as shown in Figure 1 and Figure 2 , the height of the regeneration tower 1 is H, by limiting the positions of the first liquid inlet 11, the second liquid inlet 12, and the third liquid inlet 13, the different heights of the first liquid inlet 11, the second liquid inlet 12, and the third liquid inlet 13 and the different flow rates of the condensed liquid, the first absorbent, and the second absorbent are adapted to the gradient temperature changes at different heights of the regeneration tower 1, the heat exchange efficiency is improved, and the regeneration energy consumption of the regeneration tower 1 is reduced.

[0066] For example, the value of c1 is 0.03, 0.04, 0.05, or 0.06. The value of c2 is 0.1, 0.11, 0.13, 0.15, 0.17, 0.18, 0.19, or 0.2. The value of c3 is 0.3, 0.31, 0.32, 0.35, 0.37, 0.38, 0.39, or 0.4.

[0067] In some embodiments, the size of the first liquid inlet 11 in the extension direction of the regeneration tower 1 is L1, the size of the second liquid inlet 12 in the extension direction of the regeneration tower 1 is L2, and the size of the third liquid inlet 13 in the extension direction of the regeneration tower 1 is L3, then the value of L1 is 80-120mm, the value of L2 is 300-400mm, and the value of L3 is 800-1000mm.

[0068] Specifically, as shown in Figure 1 , in the present embodiment, the liquid inlet size through the first liquid inlet 11, the second liquid inlet 12, and the third liquid inlet 13 is limited to adapt to the different liquid inlet flow rates of different liquid inlets, and the flow rates of different liquid inlets are controlled.

[0069] For example, L1, L2, and L3 refer to the hole diameter of the liquid inlet, the value of L1 is 80, 90, 100, 110, or 120, and the value in the present embodiment is 100mm. The value of L2 is 300, 320, 340, 350, 370, 390, or 400, and the value in the present embodiment is 350mm. The value of L3 is 800, 850, 900, 950, or 1000, and the value in the present embodiment is 900mm.

[0070] In the description of the present application, it is to be understood that the orientations or positional relationships indicated by the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like are based on the orientations or positional relationships shown in the drawings, and are only for the purpose of facilitating the description of the present application and simplifying the description, and do not indicate or imply that the devices or elements indicated thereby must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.

[0071] In addition, the terms "first", "second", "third", etc. are only used for descriptive purposes and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated thereby. Therefore, the features defined with "first", "second", etc. can explicitly or implicitly include at least one of the features. In the description of the present application, the meaning of "a plurality of" is at least two, such as two, three, etc., unless otherwise explicitly specified and limited.

[0072] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting", "fixing" and the like should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected or in communication with each other; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the internal communication or interaction relationship of two elements, unless otherwise explicitly limited. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0073] In the present application, unless otherwise explicitly specified and limited, the first feature is "on" or "under" the second feature, which can be direct contact between the first and second features, or indirect contact between the first and second features through an intermediate medium. Moreover, the first feature "above", "above" and "above" the second feature can be directly above or obliquely above the first feature, or only indicate that the horizontal height of the first feature is higher than that of the second feature. The first feature "below", "below" and "below" the second feature can be directly below or obliquely below the first feature, or only indicate that the horizontal height of the first feature is less than that of the second feature.

[0074] In this disclosure, the terms "one embodiment", "some embodiments", "an example", "a specific example", or "some examples" mean that a particular feature, structure, material, or characteristic is included in at least one embodiment or example of the present application. Exemplary expressions of the above terms do not necessarily refer to the same embodiment or example in this specification. Also, the described specific features, structures, materials, or characteristics can be combined in any suitable manner in one or more embodiments or examples. In addition, different embodiments or examples described in this specification and features of different embodiments or examples can be combined and combined by those skilled in the art without contradiction, if possible.

[0075] It can be understood that the above embodiments are exemplary and cannot be understood as limiting the present application, and those skilled in the art can make changes, modifications, replacements and variations to the above embodiments within the scope of the present application.

Claims

1. A carbon dioxide capture system, characterized in that, The regeneration tower includes a first liquid inlet, a second liquid inlet, and a third liquid inlet, which are arranged at intervals in the extending direction of the regeneration tower, and in the liquid flow direction, the first liquid inlet is located upstream of the second liquid inlet, and the second liquid inlet is located upstream of the third liquid inlet. The regeneration tower is provided with a tray and a packing layer. The packing layer includes a first packing layer and at least one second packing layer, which are spaced apart in the extension direction of the regeneration tower. The tray is located between the first liquid inlet and the second liquid inlet. The first liquid inlet is used to deliver condensate to the tray. The first packing layer is located between the second liquid inlet and the third liquid inlet. The second liquid inlet is used to deliver a first absorbent to the first packing layer so that the first absorbent exchanges heat with the gas between the second liquid inlet and the third liquid inlet. The third liquid inlet is used to deliver a second absorbent to the second packing layer, and the temperature of the second absorbent is higher than that of the first absorbent. It also includes a cooler having a first channel and a second channel. One end of the first channel is connected to the gas outlet of the regeneration tower, one end of the second channel is adapted to be connected to the liquid outlet of the absorption tower, and the other end of the second channel is connected to the third liquid inlet. The gas in the first channel and the liquid in the second channel can exchange heat. It also includes a heat exchanger disposed between the cooler and the regeneration tower. The heat exchanger has a third channel and a fourth channel. The third channel has a first input end, a second input end and a first output end. The first input end is connected to the liquid outlet of the absorption tower. The second input end is connected to the other end of the second channel. The first output end is connected to the third liquid inlet. The fourth channel is adapted to allow a heat source to be introduced into it. The liquid in the third channel can exchange heat with the heat source in the fourth channel. The input amount of the first input terminal is greater than the input amount of the second input terminal, and the input amount of the second input terminal is greater than the liquid inlet amount of the second liquid inlet.

2. The carbon dioxide capture system according to claim 1, characterized in that, The liquid inlet volume of the third inlet is Q2, the input volume of the first input terminal is Q21, and the input volume of the second input terminal is Q22. Then Q2 = Q21 + Q22, Q21 = a × Q2, and the value of a is 0.6-0.

8.

3. The carbon dioxide capture system according to claim 2, characterized in that, The sum of the liquid inlet volume of the second liquid inlet and the third liquid inlet is Q, and the liquid inlet volume of the second liquid inlet is Q1. Then Q1 = b1 × Q, Q2 = b2 × Q, where b1 takes the value of 0.1-0.2 and b2 takes the value of 0.8-0.

9.

4. The carbon dioxide capture system according to claim 3, characterized in that, The liquid inlet volume of the first inlet is Q0, where Q0 = b0 × Q, and b0 is 0.95%-0.1%.

5. The carbon dioxide capture system according to claim 1, characterized in that, The dimension of the second packing layer in the extension direction of the regeneration tower is larger than the dimension of the first packing layer in the extension direction of the regeneration tower; and / or, The second packing layer has a larger dimension in the radial direction of the regeneration tower than the first packing layer in the radial direction of the regeneration tower.

6. The carbon dioxide capture system according to claim 1, characterized in that, The distance between the bottom and top of the regeneration tower is H, the distance between the first inlet and the top is H1, the distance between the second inlet and the top is H2, and the distance between the third inlet and the top is H3. Then, H1 = c1 × H, H2 = c2 × H, and H3 = c3 × H, where c1 is 0.03-0.06, c2 is 0.1-0.2, and c3 is 0.3-0.

4.

7. The carbon dioxide capture system according to claim 6, characterized in that, The dimension of the first liquid inlet in the extension direction of the regeneration tower is L1, the dimension of the second liquid inlet in the extension direction of the regeneration tower is L2, and the dimension of the third liquid inlet in the extension direction of the regeneration tower is L3. Then, the value of L1 is 80-120mm, the value of L2 is 300-400mm, and the value of L3 is 800-1000mm.

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