Dynamic liquid phase distribution and heat exchange function combined heat exchange liquid distributor

Abstract

The invention discloses a dynamic liquid phase distribution and heat exchange function combined heat exchange liquid distributor, which is respectively arranged below a CO2 carbon catcher close to the top of an absorption tower and the top of a desorption tower, and comprises a dynamic liquid phase distribution mechanism on the upper layer and a dynamic liquid phase heat exchange mechanism on the lower layer; the dynamic liquid phase distribution mechanism is used for uniformly distributing a rich solution of CO2 absorbed by the absorption tower and a barren solution of CO2 desorbed by the absorption tower along the radial direction and the circumferential direction of respective tower kettles; the dynamic liquid phase heat exchange mechanism is used for calculating the cooling heat load ratio K of an outer ring and an inner ring of the dynamic liquid phase heat exchange mechanism, and the rotating speed of the dynamic liquid phase distribution mechanism is adjusted according to the cooling heat load ratio K. A novel compression energy mode is innovatively adopted, the function of a dynamic rotating liquid phase distributor is combined, the compression energy recycling problem is solved, the purpose of uniform liquid distribution is achieved, and the dynamic liquid distribution effect is fed back by means of relative changes of heat loads of an auxiliary inner / outer ring heat exchanger below the liquid distributor.

Description

Technical Field

[0001] The present invention belongs to the technical field of carbon capture, and in particular relates to a heat exchange liquid distributor combining dynamic liquid phase distribution and heat exchange functions. Background Art

[0002] In the actual CCUS engineering application projects under the background of "carbon peak and carbon neutrality", the demand for product CO2 often fluctuates greatly, which requires the CO2 capture system to frequently and significantly reduce its load for production. Under the condition that the CO2 capture system frequently and significantly reduces its load for production, the design of the CO2 capture system faces the following difficulties:

[0003] One of the difficulties is that when the demand for product CO2 drops significantly and the amount of absorption liquid entering the carbon capture tower decreases significantly, it is difficult to achieve uniformity of the absorption liquid entering the tower. Since the absorption liquid is a highly viscous liquid, when it is injected into the tower, it is generally injected from the middle and spreads to the surroundings. When its amount is relatively small, the amount of absorption liquid in the middle of the tower will be relatively large, while the amount of absorption liquid at the edge of the tower will be relatively small, resulting in difficulty in achieving uniformity of the absorption liquid entering the tower. For conventional packed towers (especially structured packing), since it is difficult to achieve uniformity of the absorption liquid entering the tower, it will seriously affect the gas-liquid contact and mass transfer effect.

[0004] The second difficulty is that when the demand for product CO2 drops significantly and the amount of absorption liquid entering the carbon capture tower decreases significantly, there is a lack of online methods to judge the uniformity of the liquid phase after the load drops. The method for judging the uniformity of the liquid phase in conventional CO2 capture systems is carried out when the demand for carbon capture is relatively large. When the demand for carbon capture is relatively large, the amount of absorption liquid injected into the tower is sufficient. When the amount of absorption liquid is sufficient, it can rely on its own flow to achieve the natural spread of the absorption liquid from the middle to the surroundings. However, when the amount of absorption liquid injected is relatively small, it cannot rely on its own flow to achieve radial uniformity. At this time, it is difficult to judge the uniformity of the current absorption liquid along the radial direction.

[0005] The third difficulty is that the temperature of the liquid phase entering the tower is sometimes high and needs to be cooled or condensed at the top of the tower. For example, in CO2 capture technology, the liquid temperature of the absorption tower can reach 60-70℃, while the absorption can only play an efficient role at a low temperature such as around 40℃. At the same time, the gas phase discharged from the top of the absorption tower carries a large amount of absorbent and also needs to be condensed. The conventional method uses cooling outside the tower, but this method has a single effect and does not take into account the condensation requirements of the gas at the top of the absorption tower. Summary of the invention

[0006] In order to solve the problems existing in the prior art, the present invention proposes a heat exchange liquid distributor combining dynamic liquid phase distribution and heat exchange function. The first purpose is to solve the problem that when the amount of absorption liquid entering the carbon capture tower is relatively small, it is difficult to achieve uniformity of the absorption liquid entering the tower; the second purpose is to solve the current problem of lack of online judgment of the uniformity of the liquid phase after the load is reduced; the third purpose is to solve the problem that when the temperature of the liquid phase entering the tower is high, the cooling effect of the outside of the tower is not good enough.

[0007] The present invention proposes the following technical solutions to solve the technical problems:

[0008] A heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange functions, characterized in that: the heat exchange liquid distributor is arranged below the top of the tower kettle of a CO2 carbon capture tower (11) and a desorption tower (14), respectively; the heat exchange liquid distributor comprises a dynamic liquid phase distribution mechanism and an auxiliary inner / outer ring heat exchange mechanism arranged below the dynamic liquid phase distribution mechanism; the dynamic liquid phase distribution mechanism is used to online adjust the uniformity of the outer ring and inner ring liquid phase of the absorption tower (11) or the desorption tower (14); the auxiliary inner / outer ring heat exchange mechanism is used to online determine ... The uniformity of the liquid phase between the outer ring and the inner ring of the absorption tower (11) or the desorption tower (14); the auxiliary inner / outer ring heat exchange mechanism is a multi-layer annular heat exchange channel corresponding to the multi-layer annular weir flow channel, and the multi-layer annular heat exchange channel includes an inner ring heat exchange channel and an outer ring heat exchange channel; the inner ring heat exchange channel and the outer ring heat exchange channel are used to calculate the cooling heat load ratio K between the outer ring and the inner ring of the absorption tower (11) or the desorption tower (14), and the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower (11) or the desorption tower (14) is adjusted according to the cooling heat load ratio K.

[0009] Furthermore, the dynamic liquid phase distribution mechanism is divided into a liquid separation component driving support (17-16) and a plurality of liquid separation component driven supports (17-15) arranged in an upper, middle, lower and circumferential direction: the upper layer is a liquid inlet pipe (17-13), the middle layer is a liquid separation component (17-12), and the lower layer is a weir flow component (17-11); the liquid separation component driving support (17-16) is used to drive the liquid separation component (17-12), and the plurality of liquid separation component driven supports (17-15) are driven by the liquid separation component (17-12).

[0010] Furthermore, the liquid inlet pipe (17-13) on the upper layer of the dynamic liquid phase distribution mechanism horizontally penetrates the tower equipment wall (17-14) from the outside to the inside, and then turns 90 degrees at the center of the absorption tower (11) or the desorption tower (14) to connect downward to the liquid separation component (17-12).

[0011] Furthermore, the liquid separation component (17-12) in the middle layer of the dynamic liquid phase distribution mechanism comprises a liquid separation component inlet (17-1202), a liquid separation branch pipe (17-1201), a liquid separation branch pipe (17-1204) and a liquid separation box (17-1203); the liquid separation component inlet (17-1202) is connected to the liquid inlet pipe (17-13) upwardly and to the liquid separation box (17-1203) downwardly.

[0012] Furthermore, the liquid separation branch pipe (17-1201) is four cross-crossed liquid separation channels uniformly arranged along the circumferential direction and the radial direction in the absorption tower (11) and the desorption tower (14), and the four cross-crossed liquid separation channels lead to the liquid separation box (17-1203) at the center of the absorption tower (11) and the desorption tower (14) respectively; the lower surface of each liquid separation branch pipe (17-1201) is also vertically connected to a plurality of liquid separation branch pipes (17-1204) along the radial direction, and the liquid separation branch pipe (17-1204) on the lower surface of each liquid separation branch pipe (17-1201) is used to connect the weir flow components (17-11) closely attached to the lower part and both sides of the liquid separation branch pipe (17-1204).

[0013] Furthermore, the weir flow component (17-11) of the lower layer of the dynamic liquid phase distribution mechanism is a multi-layer annular weir flow channel uniformly arranged along the radial and circumferential directions, and the multiple annular weir flow channels are arranged in order from the largest radius to the smallest radius: a first layer weir flow channel (17-1101), a second layer weir flow channel (17-1102), a third layer weir flow channel (17-1103), a fourth layer weir flow channel (17-1104), and an interlayer connecting weir flow channel (17-1105) that runs through the four weir flow channels along the radial direction; the multi-layer annular weir flow channel is connected to the multiple liquid separation branch pipes (17-1204) on each liquid separation branch pipe (17-1201) upwardly, and is connected to the heat exchange pipe corresponding to each liquid separation branch pipe (17-1204) downwardly.

[0014] Furthermore, the auxiliary inner / outer ring heat exchange mechanism is a multi-layer annular heat exchange channel corresponding to the multi-layer annular weir flow channel, and the inner ring heat exchange channel includes: an inner ring heat exchange inlet (17-1003), an inner ring heat exchange outlet (17-1004) and a heat exchange pipe (17-1005) connecting the inlet and the outlet; the outer ring heat exchange channel includes an outer ring heat exchange inlet (17-1001), an outer ring heat exchange outlet (17-1002) and a heat exchange pipe (17-1005) connecting the inlet and the outlet.

[0015] Furthermore, the liquid separation component driving support (17-16) is provided with an output shaft side (17-1701) and an input shaft side (17-1702) along the horizontal direction; a high-pressure air inlet (17-1703) at the upper end and a low-pressure exhaust port (17-1704) at the lower end are provided along the vertical direction; a driving blade (17-1706) is provided below the high-pressure air inlet (17-1703), and a driving machine housing (17-1707) is provided around the driving blade (17-1706); a driving machine housing (17-1707) and the output shaft side (17-1701) are provided. A bearing and a sealing mechanism (17-1708) and a bearing and a sealing mechanism (17-1709) are respectively provided at the connection between the input shaft side (17-1702); the input shaft side (17-1702) is used to connect other driving forces, including an electric motor, to ensure that the liquid separation component (17-12) can operate normally when there is no pneumatic power or the pneumatic power is insufficient; the output shaft side (17-1701) is used to connect the driving meshing gear (17-1602); the high-pressure air inlet (17-1703) is connected to a compressed air source pipeline, and the low-pressure exhaust port (1704) is connected to an exhaust pipeline.

[0016] Furthermore, the cooling heat load ratio K adjusts the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower (11) or the desorption tower (14), and the specific process is as follows:

[0017] 1) Assume that the cooling heat load of the outer ring heat exchange channel is Q1 = CP1*m1*ΔT1; the cooling heat load of the inner ring heat exchange channel is Q2 = CP2*m2*ΔT2; where CP is the constant pressure specific heat capacity of the cooling medium, m is the mass flow rate of the cooling medium, and ΔT is the temperature difference of the cooling medium after heat exchange;

[0018] 2) K = Q1 / Q2 is the cooling heat load ratio of the outer ring and the inner ring;

[0019] 3) When the liquid phase is distributed evenly, K is an obtainable operating experience value k0. When it is uneven, K>k0, or K<k0;

[0020] 4) According to K>k0 or K<k0, adjust the K value so that the K value is close to the empirical value k0.

[0021] Advantages and effects of the present invention

[0022] 1. The present invention uses an attached inner / outer ring heat exchange mechanism to online judge the uniformity of the liquid phase between the outer ring and the inner ring of the absorption tower or desorption tower, and uses a dynamic liquid phase distribution mechanism to online adjust the uniformity of the liquid phase between the outer ring and the inner ring of the absorption tower or desorption tower, thereby solving the problem that when the demand for CO2 products fluctuates greatly and the amount of absorption liquid entering the tower is relatively small, it is difficult to achieve uniformity of the absorption liquid entering the tower.

[0023] 2. The present invention organically combines dynamic liquid phase distribution with heat exchange functions, and uses the relative change of heat load of the inner / outer ring heat exchange mechanism under the dynamic rotating liquid phase distributor to feedback the effect of dynamic liquid distribution, thereby solving the problem that the prior art lacks online judgment of the uniformity of the liquid phase after the load decreases.

[0024] 3. The auxiliary inner / outer ring heat exchange mechanism of the present invention not only solves the problem of online judgment of the uniformity of the outer and inner ring liquid phases of the absorption tower or desorption tower, but also integrates the heat exchange mechanism inside the tower to solve the problem that when the temperature of the liquid phase entering the tower is high, the cooling effect of the outside of the tower is not good enough. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is the process system diagram of the present invention;

[0026] Figure 2 This is a diagram of a heat exchange liquid distributor of the present invention;

[0027] Figure 3 This is a diagram of the heat exchange component of the present invention;

[0028] Figure 4 This is a diagram of the weir flow component of the present invention;

[0029] Figure 5 This is a connection diagram of the heat exchange component and the weir flow component of the present invention;

[0030] Figure 6 It is a diagram of the liquid separation component of the present invention;

[0031] Figure 7 This is a driven support diagram of the liquid separation component of the present invention;

[0032] Figure 8 A diagram showing the connection relationship between the liquid separation component and the driving support of the liquid separation component of the present invention;

[0033] Fig. 9 This is a diagram of the gas residual pressure driving device of the present invention;

[0034] In the figure: 10: raw gas compressor; 11: absorption tower; 12: rich liquid circulation pump; 13: lean and rich liquid heat exchanger; 14: desorption tower; 15: desorption tower heater; 16: lean liquid circulation pump; 111: absorption tower liquid inlet rotary distributor; 112: absorption tower attached inner ring heat exchange channel; 113: absorption tower attached outer ring heat exchange channel; 101: compressor gas residual pressure driving source; 114: absorption tower gas residual pressure driving source; 141: desorption tower liquid inlet rotary distributor; 142: desorption tower attached inner ring heat exchange channel; 143: desorption tower attached outer ring heat exchange channel; 144: desorption tower gas residual pressure driving source;

[0035] 17-10: heat exchange component; 17-1001: outer ring heat exchange inlet; 17-1002: outer ring heat exchange outlet; 17-1003: inner ring heat exchange inlet; 17-1004: inner ring heat exchange outlet; 17-1005: heat exchange pipeline;

[0036] 17-11: weir flow component; 17-1101: first layer weir flow channel; 17-1102: second layer weir flow channel; 17-1103: third layer weir flow channel; 17-1104: fourth layer weir flow channel; 17-1105: interlayer connecting weir flow channel; 17-1106: connecting plate;

[0037] 17-12: liquid separation component; 17-1201: liquid separation branch pipe; 17-1202: liquid separation component inlet; 17-1203: liquid separation box; 17-1204: branch pipe; 17-1205: liquid separation branch pipe connecting ring plate; 17-1206: annular flat gear under the ring plate;

[0038] 17-13: liquid inlet pipe; 17-14: tower equipment wall;

[0039] 17-15: driven support of liquid separation component; 17-1501: bearing structure of support section;

[0040] 17-16: driving support of liquid separation component; 17-1601: driving shaft; 17-1602: driving gear; 17-1603: bearing and sealing mechanism;

[0041] 17-1701: output shaft side; 17-1702: input shaft side; 17-1703: high-pressure air inlet; 17-1704: low-pressure exhaust port; 17-1705: condensate discharge port; 17-1706: drive blades; 17-1707: drive motor housing; 17-1708: bearings and sealing mechanism; 17-1709: bearings and sealing mechanism. DETAILED DESCRIPTION

[0042] 1. Innovation of the present invention: Innovation point 1: The present invention organically combines dynamic liquid phase distribution with heat exchange functions, and uses the relative change of heat load of the attached inner / outer ring heat exchange mechanism below the dynamic rotating liquid phase distributor to feedback the effect of dynamic liquid distribution. The effect of feedback dynamic liquid distribution is to dynamically adjust the rotation speed of the dynamic rotating liquid phase distributor 111 of the absorption tower or the dynamic rotating liquid phase distributor 141 of the desorption tower according to the ratio K of the inner and outer ring cooling heat loads. Innovation point 2: Move the heat exchanger from outside the tower to inside the tower. The attached inner / outer ring heat exchange mechanism of the present invention is arranged inside the absorption tower 11 and the desorption tower 14, which not only plays a role in assisting uniform liquid distribution, but also moves the heat exchanger from outside the tower to inside the tower. Its advantage is that the condensed absorbent directly returns to the tower, reducing equipment and pipelines.

[0043] 2. The difference between the present invention and the prior art: the liquid phase distributor of the present invention not only has the function of rotating liquid distribution energy supply, but also has a heat exchange mechanism (an inner ring heat exchange channel 112 attached to the absorption tower and an outer ring heat exchange channel 113 attached to the absorption tower, an inner ring heat exchange channel 142 attached to the desorption tower and an outer ring heat exchanger 143 attached to the desorption tower). The heat exchange mechanism is divided into an inner ring heat exchange mechanism and an outer ring heat exchange mechanism. The inner ring heat exchange mechanism is used to judge the heat exchange conditions close to the center of the absorption tower or the desorption tower, and the outer ring heat exchange mechanism is used to judge the heat exchange conditions far away from the center of the absorption tower or the desorption tower. The rotation speed of the dynamic liquid phase distribution mechanism is adjusted by the ratio K between them, and then the uniformity of the outer ring and inner ring liquid phases of the absorption tower 11 or the desorption tower 14 is dynamically adjusted.

[0044] 3. Design principle of the present invention

[0045] Design principle of the attached inner / outer ring heat exchange mechanism: Under the condition of uniform liquid distribution, the cooling heat load ratio K of the inner / outer ring heat exchange channel is relatively fixed, and an empirical value k0 can be obtained based on experience. When unevenness occurs, the cooling heat load ratio will deviate from the empirical value k0. When it deviates from the empirical value k0, it will be adjusted by the absorption tower liquid inlet rotary liquid distributor 111 or the absorption tower liquid inlet rotary liquid distributor 141. The cooling heat load ratio will deviate from the normal value when unevenness occurs, as follows: Assume that the cooling heat load of the outer ring heat exchange channel Q1 = CP1*m1*ΔT1; the cooling heat load of the inner ring heat exchanger Q2 = CP2*m2*ΔT2; where CP is the constant pressure specific heat capacity of the cooling medium, m is the mass flow rate of the cooling medium, and ΔT is the temperature difference of the cooling medium after heat exchange. K = Q1 / Q2 is the cooling heat load ratio of the outer ring and the inner ring. When the liquid phase is distributed more evenly, such as the inner ring liquid phase is larger, ΔT is larger under the same m, then Q1 increases, Q2 decreases, k>k0; in the opposite direction, k<k0, therefore, the speed of the current absorption tower liquid inlet rotary distributor 111 or the absorption tower liquid inlet rotary distributor 141 is dynamically adjusted through the ratio K: adjusting the speed is to adjust the magnitude of the centrifugal force, and the purpose of adjusting the liquid phase uniformity is achieved by adjusting the magnitude of the centrifugal force.

[0046] Based on the above invention principle, the present invention designs a heat exchange liquid distributor combining dynamic liquid phase distribution and heat exchange function, which is characterized in that: the heat exchange liquid distributor is arranged below the top of the tower kettle of the CO2 carbon capture tower 11 and the desorption tower 14 respectively, and the heat exchange liquid distributor includes a dynamic liquid phase distribution mechanism and an auxiliary inner / outer ring heat exchange mechanism arranged below the dynamic liquid phase distribution mechanism; the dynamic liquid phase distribution mechanism is used to online adjust the uniformity of the outer ring and inner ring liquid phases of the absorption tower 11 or the desorption tower 14; the auxiliary inner / outer ring heat exchange mechanism is used to online judge the uniformity of the outer ring and inner ring liquid phases of the absorption tower 11 or the desorption tower 14; the multi-layer annular heat exchange channel includes an inner ring heat exchange channel and an outer ring heat exchange channel; the inner ring heat exchange channel and the outer ring heat exchange channel are used to calculate the cooling heat load ratio K of the outer ring and the inner ring of the absorption tower 11 or the desorption tower 14, and adjust the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower 11 or the desorption tower 14 according to the cooling heat load ratio K.

[0047] like Figure 2 As shown, the dynamic liquid phase distribution mechanism is divided into upper, middle, lower and circumferentially arranged liquid separation component driving supports 17-16 and multiple liquid separation component driven supports 17-15: the upper layer is the liquid inlet pipe 17-13, the middle layer is the liquid separation component 17-12, and the lower layer is the weir flow component 17-11; the liquid separation component driving support 17-16 is used to drive the liquid separation component 17-12, and the multiple liquid separation component driven supports 17-15 are driven by the liquid separation component 17-12.

[0048] like Figure 2 As shown, the liquid inlet pipe 17-13 on the upper layer of the dynamic liquid phase distribution mechanism horizontally penetrates the tower equipment wall 17-14 from the outside to the inside, turns 90 degrees at the center of the absorption tower 11 or the desorption tower 14 and connects to the liquid separation component 17-12 downward.

[0049] like Figure 2 As shown, the liquid separation component 17-12 in the middle layer of the dynamic liquid phase distribution mechanism includes a liquid separation component inlet 17-1202, a liquid separation branch pipe 17-1201, a branch pipe 17-1204 and a liquid separation box 17-1203; the liquid separation component inlet 17-1202 is connected to the liquid inlet pipe 17-13 upward and to the liquid separation box 17-1203 downward.

[0050] like Figure 5 , Figure 6As shown, the liquid separation pipe 17-1201 is four cross-shaped liquid separation channels uniformly arranged along the circumferential direction and the radial direction in the absorption tower 11 and the desorption tower 14, and the four cross-shaped liquid separation channels lead to the liquid separation box 17-1203 at the center of the absorption tower 11 and the desorption tower 14 respectively; the lower surface of each liquid separation pipe 17-1201 is also vertically connected to a plurality of branch pipes 17-1204 along the radial direction, and the branch pipes 17-1204 on the lower surface of each liquid separation pipe 17-1201 are used to connect the weir flow components 17-11 close to the lower part and both sides of the branch pipes 17-1204.

[0051] like Figure 2 , Figure 5 As shown, the weir flow component 17-11 of the lower layer of the dynamic liquid phase distribution mechanism is a multi-layer annular weir flow channel uniformly arranged along the radial and circumferential directions, and the multiple annular weir flow channels are arranged in order from large radius to small radius: a first layer weir flow channel 17-1101, a second layer weir flow channel 17-1102, a third layer weir flow channel 17-1103, a fourth layer weir flow channel 17-1104 and an interlayer connecting weir flow channel 17-1105 that runs through the four weir flow channels along the radial direction; the multi-layer annular weir flow channels are connected to multiple branch pipes 17-1204 on each liquid distribution pipe 17-1201 upwardly, and are connected to the heat exchange pipes corresponding to each branch pipe 17-1204 downwardly.

[0052] like Figure 3 As shown, the inner ring heat exchange channel includes: an inner ring heat exchange inlet 17-1003, an inner ring heat exchange outlet 17-1004 and a heat exchange pipe 17-1005 connecting the inlet and the outlet; the outer ring heat exchange channel includes an outer ring heat exchange inlet 17-1001, an outer ring heat exchange outlet 17-1002 and a heat exchange pipe 17-1005 connecting the inlet and the outlet.

[0053] like Fig. 9As shown, the liquid separation component driving support 17-16 is provided with an output shaft side 17-1701 and an input shaft side 17-1702 in the horizontal direction; a high-pressure air inlet 17-1703 at the upper end and a low-pressure exhaust port 17-1704 at the lower end are provided in the vertical direction; a driving blade 17-1706 is provided below the high-pressure air inlet 17-1703, and a driving machine housing 17-1707 is provided around the driving blade 17-1706; between the driving machine housing 17-1707 and the output shaft side 17-1701 and the input shaft The connection of the side 17-1702 is respectively provided with a bearing and a sealing mechanism 17-1708 and a bearing and a sealing mechanism 17-1709; the input shaft side 17-1702 is used to connect other driving forces, including an electric motor, to ensure that the liquid separation component 17-12 can operate normally when there is no pneumatic power or the pneumatic power is insufficient; the output shaft side 17-1701 is used to connect the driving meshing gear 17-1602; the high-pressure air inlet 17-1703 is connected to a compressed air source pipeline, and the low-pressure exhaust port 17-1704 is connected to an exhaust pipeline.

[0054] The cooling heat load ratio K adjusts the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower (11) or the desorption tower (14), and the specific process is as follows:

[0055] 1) Assume that the cooling heat load of the outer ring heat exchange channel is Q1 = CP1*m1*ΔT1; the cooling heat load of the inner ring heat exchanger is Q2 = CP2*m2*ΔT2; where CP is the constant pressure specific heat capacity of the cooling medium, m is the mass flow rate of the cooling medium, and ΔT is the temperature difference of the cooling medium after heat exchange;

[0056] 2) K = Q1 / Q2 is the cooling heat load ratio of the outer ring and the inner ring;

[0057] 3) When the liquid phase is distributed evenly, K is an obtainable operating experience value k0. When it is uneven, K>k0, or K<k0;

[0058] 4) According to K>k0 or K<k0, adjust the K value so that the K value is close to the empirical value k0.

[0059] Embodiment 1

[0060] The present invention uses the above-mentioned heat exchange liquid distributor combining dynamic liquid phase distribution and heat exchange function, and also designs a carbon dioxide absorption method based on boosting benefit, which includes the following steps:

[0061] Step 1: Figure 1 As shown, the CO2-containing gas is compressed to a set pressure by the raw gas compressor 10, and then enters the absorption tower 11, where it reacts with the absorption liquid flowing down from the top of the absorption tower 11 in gas and liquid phases to generate a rich liquid that absorbs CO2;

[0062] Step 2: Figure 2 As shown, the remaining inert gas enters the gas residual pressure driving device in the absorption tower 11 as the backup power of the corresponding device; the corresponding device is: the raw gas compressor 10, the absorption tower liquid inlet rotary liquid distributor 111 and the desorption tower liquid inlet rotary liquid distributor 141; the backup power is: the original motor drive of the corresponding device is used as the first driving force, and the gas residual pressure drive of the corresponding device is used as the second driving force;

[0063] Supplementary Note 1:

[0064] The remaining inert gas does not need to be compressed, but as the CO2 gas is compressed, the remaining inert gas is compressed. This application utilizes this part of the compressed remaining inert gas. Figure 1 There are three residual pressure driving devices, namely, compressor gas residual pressure driving source 101, compressor gas residual pressure driving source 114, and desorption tower gas residual pressure driving source 144, which are respectively connected to the raw gas compressor 10, the absorption tower liquid inlet rotary liquid distributor 111, and the desorption tower liquid inlet rotary liquid distributor 141, wherein the absorption tower gas residual pressure driving source 114 serves as the second driving source of the absorption tower liquid inlet rotary liquid distributor 111; the desorption tower gas residual pressure driving source 144 serves as the second driving source of the desorption tower liquid inlet rotary liquid distributor 141;

[0065] Step 3: The rich liquid that absorbs CO2 is discharged from the bottom of the absorption tower 11, passes through the channel valve 123, and then passes through the lean and rich liquid heat exchanger 13 from top to bottom into the desorption tower 14;

[0066] Supplementary Note 2:

[0067] like Figure 1 As shown, under normal circumstances, the channels of the channel valve 121, the rich liquid circulation pump 12 and the channel valve 122 are not used frequently and are only used during system startup or emergency situations. This embodiment adopts a method of increasing pressure to increase the dissolution rate, which not only reduces the inner diameter of the absorption tower but also saves the circulation pump 121.

[0068] Step 4, the rich liquid absorbed by CO2 entering the desorption tower 14 is desorbed by the desorption tower through the desorption tower liquid inlet rotary liquid distribution device, and the desorbed CO2 gas is discharged from the top of the desorption tower 14; the desorption tower liquid inlet rotary liquid distribution device is used to evenly distribute the CO2 rich liquid entering the desorption tower 14 along the radial and circumferential directions of the desorption tower 14; the absorption tower liquid inlet rotary liquid distribution device includes an upper and lower layer, the upper layer is the absorption tower liquid inlet rotary liquid distributor 111, and the lower layer is a heat exchange mechanism, which is composed of an absorption tower attached inner ring heat exchange channel 112 and an absorption tower attached outer ring heat exchanger 113 arranged below the absorption tower liquid inlet rotary liquid distributor 111; the absorption tower attached inner ring heat exchange channel 112 and the absorption tower attached outer ring heat exchanger 113 are used to calculate the outer ring and inner ring cooling heat load ratio K, and adjust the rotation speed of the absorption tower liquid inlet rotary liquid distributor (111) according to the cooling heat load ratio K.

[0069] Supplementary Note 3:

[0070] like Figure 1 As shown, the absorption tower attached inner ring heat exchange channel 112 is located in the middle, and the absorption tower attached outer ring heat exchanger 113 is located at the two sides, which represent the liquid phase density in the center area and the large radius of the tower body, respectively.

[0071] Step 5: Figure 1 As shown, the lean liquid for desorbing CO2 passes through the lean liquid circulation pump 16 and the lean-rich liquid heat exchanger 13, and enters the absorption tower liquid inlet rotary liquid distribution device of the absorption tower 11 from top to bottom to complete the circulation of the liquid phase; the absorption tower liquid inlet rotary liquid distribution device is used to evenly distribute the CO2 lean liquid entering the absorption tower 11 along the radial and circumferential directions of the absorption tower; the desorption tower liquid inlet rotary liquid distribution device includes an upper and lower layer, the upper layer is the absorption tower liquid inlet rotary liquid distributor 141, and the lower layer is a heat exchange mechanism, which is composed of a desorption tower attached inner ring heat exchange channel 142 and a desorption tower attached outer ring heat exchanger 143 arranged below the absorption tower liquid inlet rotary liquid distributor 141; the desorption tower attached inner ring heat exchange channel 142 and the desorption tower attached outer ring heat exchanger 143 are used to calculate the outer ring and inner ring cooling heat load ratio K, and adjust the rotation speed of the absorption tower liquid inlet rotary liquid distributor 141 according to the cooling heat load ratio K.

[0072] Supplementary Note 4:

[0073] like Figure 2 As shown, since the liquid phase enters from the central area, if there is no absorption tower liquid inlet rotating liquid distribution device or analysis tower liquid inlet rotating liquid distribution device, the central area will have high density and low density in the surrounding area, which is uneven. The purpose of using the absorption tower liquid inlet rotating liquid distribution device or the analysis tower liquid inlet rotating liquid distribution device is to use the principle of centrifugal force to diffuse the liquid phase with high density in the middle from the central area to the surrounding area, so as to achieve the purpose of uniform distribution.

[0074] like Figure 1 As shown, the gas residual pressure driving device includes three: a compressor gas residual pressure driving device 101 for driving the raw gas compressor 10; an absorption tower liquid distributor gas residual pressure driving device 114 for driving the absorption tower liquid inlet rotary liquid distributor 111; and a desorption tower liquid distributor gas residual pressure driving device 144 for driving the desorption tower liquid inlet rotary liquid distributor 141.

[0075] like Figure 1 As shown, the gas residual pressure drive serves as the second driving force, specifically: the compressor gas residual pressure driving device 101 serves as the second driving force of the raw gas compressor 10; the absorption tower liquid distributor gas residual pressure driving device 114 serves as the second driving force for driving the absorption tower liquid inlet rotary liquid distributor 111; the desorber tower liquid distributor gas residual pressure driving device 144 serves as the second driving force for the desorber tower liquid inlet rotary liquid distributor 141; after the absorption tower liquid distributor gas residual pressure driving device 114 and the desorber tower liquid distributor gas residual pressure driving device 144 drive the absorption tower liquid inlet rotary liquid distributor 111 and the desorber tower liquid inlet rotary liquid distributor 141 respectively, the gas expands and the temperature drops, accompanied by condensate, which is rich in absorbent, thereby returning the absorbent to the desorber.

[0076] like Figure 2 As shown, the absorption tower liquid inlet rotary liquid distributor 111 or the desorption tower liquid inlet rotary liquid distributor 141 includes three layers of upper, middle and lower layers and circumferentially arranged liquid separation component driving supports 17-16 and multiple liquid separation component driven supports 17-15: the upper layer is the liquid inlet pipe 17-13, the middle layer is the liquid separation component 17-12, and the lower layer is the weir flow component 17-11; the liquid separation component driving support 17-16 is used to drive the liquid separation component 17-12 to rotate; the multiple liquid separation component driven supports 17-15 are used to be driven by the liquid separation component 17-12.

[0077] like Figure 2 As shown, the liquid inlet pipe 17-13 horizontally penetrates the tower equipment wall 17-14 from the outside to the inside, and then turns 90 degrees downward at the center of the absorption tower or desorption tower to connect with the liquid separation component 17-12.

[0078] like Figure 2As shown, the liquid separation component 17-12 includes a liquid separation component inlet 17-1202, a liquid separation branch pipe 17-1201, a branch pipe 17-1204 and a liquid separation box 17-1203; the liquid separation component inlet 17-1202 is connected to the liquid inlet pipe 17-13 upwardly, and is connected to the liquid separation box 17-1203 and the liquid separation branch pipe 17-1201 downwardly; the liquid separation branch pipe 17-1201 is four cross-shaped liquid separation channels uniformly arranged along the circumferential direction and the radial direction in the absorption tower, and the four liquid separation channels are connected to the liquid separation box 17-1203 in the central area respectively; the lower surface of each liquid separation branch pipe 17-1201 is also vertically connected to a plurality of branch pipes 17-1204, and the branch pipes 17-1204 are used to connect the weir flow component 17-11 of the lower layer.

[0079] like Figure 2 , Figure 4 As shown, the weir flow component 17-11 is a plurality of annular channels uniformly arranged along the radial and circumferential directions; the plurality of annular channels are connected to the liquid separation branch pipe 1204 upwards and to the heat exchange mechanism of the absorption tower liquid inlet rotating liquid distribution device downwards; the plurality of annular channels are arranged in order from large radius to small radius: a first layer weir flow channel 17-1101, a second layer weir flow channel 17-1102, a third layer weir flow channel 17-1103, a fourth layer weir flow channel 17-1104 and an interlayer connecting weir flow channel 17-1105 running through the four weir flow channels.

[0080] like Figure 2 , Figure 3 As shown, the absorption tower-affiliated inner ring heat exchange channel 112 arranged below the absorption tower inlet rotary liquid distributor 111 includes: an inner ring heat exchange inlet 17-1003, an inner ring heat exchange outlet 17-1004 and a heat exchange pipe 17-1005 connecting the inlet and the outlet; the absorption tower-affiliated outer ring heat exchanger 113 arranged below the absorption tower inlet rotary liquid distributor 111 includes: an outer ring heat exchange inlet 17-1001, an outer ring heat exchange outlet 17-1002 and a heat exchange pipe 17-1005 connecting the inlet and the outlet.

[0081] The rotation speed of the absorption tower liquid inlet rotary distributor 111 is adjusted according to the cooling heat load ratio K, or the rotation speed of the absorption tower liquid inlet rotary distributor 141 is adjusted according to the cooling heat load ratio K. The specific process is as follows:

[0082] 1) Assume that the cooling heat load of the outer ring heat exchanger is Q1 = CP1*m1*ΔT1; the cooling heat load of the inner ring heat exchanger is Q2 = CP2*m2*ΔT2; where CP is the constant pressure specific heat capacity of the cooling medium, m is the mass flow rate of the cooling medium, and ΔT is the temperature difference of the cooling medium after heat exchange;

[0083] 2) K = Q1 / Q2 is the cooling heat load ratio of the outer ring and the inner ring;

[0084] 3) When the liquid phase is distributed evenly, K is an obtainable operating experience value k0. When it is uneven, K>k0, or K<k0;

[0085] 4) According to K>k0 or K<k0, adjust the K value so that the K value is close to the empirical value k0.

[0086] The above contents are merely examples and explanations of the concept of the present invention. The technicians in this technical field may make various modifications or additions to the specific embodiments described or replace them in a similar manner. As long as they do not deviate from the concept of the invention or exceed the scope defined by the claims, they should all fall within the protection scope of the present invention.

Claims

1. A heat exchange liquid distributor combining dynamic liquid phase distribution and heat exchange functions, characterized in that: The heat exchange liquid distributor is arranged below the top of the tower kettle of the CO2 carbon capture device near the absorption tower (11) and the desorption tower (14), and the heat exchange liquid distributor comprises a dynamic liquid phase distribution mechanism and an auxiliary inner / outer ring heat exchange mechanism arranged below the dynamic liquid phase distribution mechanism; the dynamic liquid phase distribution mechanism is used to adjust the uniformity of the outer ring and inner ring liquid phase of the absorption tower (11) or the desorption tower (14) online; the auxiliary inner / outer ring heat exchange mechanism is used to judge online whether the absorption tower (11) or the desorption tower (14) is uniform. 4) the uniformity of the liquid phase between the outer ring and the inner ring; the auxiliary inner / outer ring heat exchange mechanism is a multi-layer annular heat exchange channel corresponding to the multi-layer annular weir flow channel, and the multi-layer annular heat exchange channel includes an inner ring heat exchange channel and an outer ring heat exchange channel; the inner ring heat exchange channel and the outer ring heat exchange channel are used to calculate the cooling heat load ratio K between the outer ring and the inner ring of the absorption tower (11) or the desorption tower (14), and the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower (11) or the desorption tower (14) is adjusted according to the cooling heat load ratio K.

2. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange function according to claim 1, characterized in that: The dynamic liquid phase distribution mechanism is divided into a liquid separation component driving support (17-16) and a plurality of liquid separation component driven supports (17-15) arranged in an upper, middle, lower and circumferential direction: the upper layer is a liquid inlet pipe (17-13), the middle layer is a liquid separation component (17-12), and the lower layer is a weir flow component (17-11); the liquid separation component driving support (17-16) is used to drive the liquid separation component (17-12), and the plurality of liquid separation component driven supports (17-15) are driven by the liquid separation component (17-12).

3. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange function according to claim 2, characterized in that: The liquid inlet pipe (17-13) on the upper layer of the dynamic liquid phase distribution mechanism horizontally penetrates the tower equipment wall (17-14) from the outside to the inside, and then turns 90 degrees at the center of the absorption tower (11) or the desorption tower (14) to connect downwardly to the liquid separation component (17-12).

4. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange function according to claim 2, characterized in that: The liquid separation component (17-12) in the middle layer of the dynamic liquid phase distribution mechanism comprises a liquid separation component inlet (17-1202), a liquid separation branch pipe (17-1201), a liquid separation branch pipe (17-1204) and a liquid separation box (17-1203); the liquid separation component inlet (17-1202) is connected to the liquid inlet pipe (17-13) upwards and to the liquid separation box (17-1203) downwards.

5. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange function according to claim 4, characterized in that: The liquid separation branch pipe (17-1201) is four cross-crossed liquid separation channels uniformly arranged along the circumferential direction and the radial direction in the absorption tower (11) and the desorption tower (14), and the four cross-crossed liquid separation channels lead to the liquid separation box (17-1203) at the center of the absorption tower (11) and the desorption tower (14) respectively; the lower surface of each liquid separation branch pipe (17-1201) is also vertically connected to a plurality of liquid separation branch pipes (17-1204) along the radial direction, and the liquid separation branch pipe (17-1204) on the lower surface of each liquid separation branch pipe (17-1201) is used to connect the weir flow components (17-11) closely attached to the lower part and both sides of the liquid separation branch pipe (17-1204).

6. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange functions according to claim 5, characterized in that: The weir flow component (17-11) of the lower layer of the dynamic liquid phase distribution mechanism is a multi-layer annular weir flow channel uniformly arranged along the radial and circumferential directions, and the multiple annular weir flow channels are arranged in order from the largest radius to the smallest radius: a first layer weir flow channel (17-1101), a second layer weir flow channel (17-1102), a third layer weir flow channel (17-1103), a fourth layer weir flow channel (17-1104), and an interlayer connecting weir flow channel (17-1105) that runs through the four weir flow channels along the radial direction; the multi-layer annular weir flow channel is connected to the multiple liquid separation branch pipes (17-1204) on each liquid separation branch pipe (17-1201) upwards, and is connected to the heat exchange pipe corresponding to each liquid separation branch pipe (17-1204) downwards.

7. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange functions according to claim 3, characterized in that: The inner ring heat exchange channel includes: an inner ring heat exchange inlet (17-1003), an inner ring heat exchange outlet (17-1004) and a heat exchange pipe (17-1005) connecting the inlet and the outlet; the outer ring heat exchange channel includes an outer ring heat exchange inlet (17-1001), an outer ring heat exchange outlet (17-1002) and a heat exchange pipe (17-1005) connecting the inlet and the outlet.

8. The heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange functions according to claim 2, characterized in that: The liquid separation component driving support (17-16) is provided with an output shaft side (17-1701) and an input shaft side (17-1702) in the horizontal direction; a high-pressure air inlet (17-1703) at the upper end and a low-pressure exhaust port (17-1704) at the lower end in the vertical direction; a driving blade (17-1706) is provided below the high-pressure air inlet (17-1703), and a driving machine housing (17-1707) is provided around the driving blade (17-1706); a driving machine housing (17-1707) and an output shaft side (17-1701) and an input shaft side (17-1702) are provided between the driving machine housing (17-1707) and the output shaft side (17-1701) and the input shaft side (17-1702). The connection between the input shaft side (17-1702) and the output shaft side (17-1701) is respectively provided with a bearing and a sealing mechanism (17-1708) and a bearing and a sealing mechanism (17-1909); the input shaft side (17-1702) is used to connect other driving forces, including an electric motor, to ensure that the liquid separation component (17-12) can operate normally when there is no air pressure power or the air pressure power is insufficient; the output shaft side (17-1701) is used to connect the driving meshing gear (17-1602); the high-pressure air inlet (17-1703) is connected to a compressed air source pipeline, and the low-pressure exhaust port (17-1704) is connected to an exhaust pipeline.

9. According to the heat exchange liquid distributor with a combination of dynamic liquid phase distribution and heat exchange functions as described in claim 1, the rotation speed of the dynamic liquid phase distribution mechanism of the absorption tower (11) or the desorption tower (14) is adjusted according to the cooling heat load ratio K, and the specific process is as follows: 1) Assume that the cooling heat load of the outer ring heat exchange channel is Q1 = CP1*m1*ΔT1; the cooling heat load of the inner ring heat exchange channel is Q2 = CP2*m2*ΔT2; where CP is the constant pressure specific heat capacity of the cooling medium, m is the mass flow rate of the cooling medium, and ΔT is the temperature difference of the cooling medium after heat exchange; 2) K = Q1 / Q2 is the cooling heat load ratio of the outer ring and the inner ring; 3) When the liquid phase is distributed evenly, K is an obtainable operating experience value k0. When it is uneven, K>k0, or K<k0; 4) According to K>k0 or K<k0, adjust the K value so that the K value is close to the empirical value k0.

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