Carbon capture and absorption tower

Abstract

Carbon capture and absorption tower, characterized in that it comprises: a tower body having an absorption chamber, a pretreatment chamber, and a loaded liquid chamber, wherein a medium inlet and a flue gas outlet are provided at the top portion of the tower body, and wherein a medium outlet and a flue gas inlet are provided at the bottom portion of the tower body; a first heat exchanger component arranged in the loaded liquid chamber, wherein the flue gas inlet is connected to the first heat exchanger component to enable the flue gas entering the first heat exchanger component to exchange heat with an absorption medium in the loaded liquid chamber, and wherein the cooled flue gas enters the absorption chamber after passing through the pretreatment chamber, and wherein the heated absorption medium is discharged through the medium outlet; a second heat exchanger component arranged in the absorption chamber, wherein the medium inlet is connected to the absorption chamber, and wherein the second heat exchanger component is used to cool the absorption medium and / or the flue gas in the absorption chamber, and wherein the flue gas is discharged via the flue gas outlet after the removal of carbon dioxide and the absorption medium flows into the loaded liquid chamber after the absorption of carbon dioxide.

Description

TECHNICAL FIELDThe present invention relates to the technical field of carbon deposition, in particular to a tower for the deposition and absorption of carbon.PRIOR ARTThe separated liquid and carbon dioxide undergo a chemical absorption reaction in the absorption tower, which is an exothermic reaction. If the heat cannot be dissipated, this may result in a temperature rise in the absorption tower, which deteriorates the absorption efficiency.In the related technology, the carbon separation system for ensuring an efficient absorption reaction typically includes a flue gas desulfurization tower and a heat exchanger for cooling the flue gas and the semi-lean solution (semi-lean solution) that are entered into the absorption tower. However, the flue gas desulfurization towers and heat exchangers are external and require a large amount of space, so that they are unsuitable for retrofitting new carbon deposition plants in existing power plants. In addition, the heat energy of the flue gases cannot be utilized, resulting in waste of energy.CONTENT OF THE PRESENT INVENTIONThe present invention aims to solve one of the technical problems in the related technology at least to a certain extent.To this end, an embodiment of the present invention provides a carbon deposition and absorption tower capable of improving integration of the apparatus, reducing space, and improving flue gas heat utilization efficiency and carbon deposition absorption efficiency.A carbon deposition and absorption tower according to an embodiment of the present invention comprises:a tower body comprising an absorption chamber, a pretreatment chamber and a loaded liquid chamber (engl. Rich solution chamber), wherein a medium inlet and a flue gas outlet are provided at the tip portion of the tower body, and wherein a medium outlet and a flue gas inlet are provided at the bottom portion of the tower body;a first heat exchanger component disposed in the loaded liquid chamber, wherein the flue gas inlet is connected to the first heat exchanger component to allow the flue gas entering the first heat exchanger component to exchange heat with an absorption medium in the loaded liquid chamber, and wherein the cooled flue gas enters the absorption chamber after passing the pretreatment chamber, and wherein the heated absorption medium is discharged through the medium outlet;a second heat exchanger component arranged in the absorption chamber, wherein the medium inlet is connected to the absorption chamber, and wherein the second heat exchanger component is used to cool the absorption medium and / or the flue gas in the absorption chamber, and wherein the flue gas is discharged via the flue gas outlet after removal of carbon dioxide and the absorption medium flows into the chamber of the rich liquid after absorption of carbon dioxide.In some embodiments, the carbon deposition and absorption tower further comprises a fill layer disposed in the absorption chamber, the fill layer disposed below the second heat exchanger component.In some embodiments, the number of second heat exchanger components and the filling layers are each a plurality, wherein the plurality of second heat exchanger components are spaced apart along the flow direction of the absorption medium, and wherein the plurality of filling layers are spaced apart along the flow direction of the absorption medium;and wherein the filling layers and the second heat exchanger components are arranged one-to-one correspondingly, and wherein the filling layer is arranged below the corresponding second heat exchanger component.In some embodiments, the carbon deposition and absorption tower further comprises a temperature sensing component and a control component, wherein the temperature sensing component is used to sense the temperature of the absorption medium flowing into the filling layer, and wherein the control component is connected to the second heat exchange component, and wherein the control component is used to control the flow rate of the heat exchange medium in the second heat exchange component such that the temperature of the absorption medium entering the filling layer is less than a first threshold.In some embodiments, the first heat exchanger component comprises a base body and a plurality of first tubes, wherein the base body has a first chamber, and wherein the flue gas inlet is connected to the first chamber, and wherein the base body is arranged in the loaded liquid chamber, and wherein one end of the first tube is connected to the first chamber and the other end of the first tube is connected to the pretreatment chamber.In some embodiments, the plurality of first tubes are distributed in an array and at intervals in the loaded liquid chamber; and / or the first heat exchanger component further comprises a plurality of baffle plates, the plurality of baffle plates being distributed in the first chamber to disperse and deflect the flue gas entering the first chamber through the flue gas inlet; and / or the number of flue gas inlets is a plurality, the plurality of flue gas inlets being distributed at intervals along the circumferential direction of the base body; and / or a flow gap is formed between the circumferential sidewall of the base body and the inner wall of the loaded liquid chamber; and / or the central part of the main body has a flow channel, wherein one end of the flow channel is connected to the loaded liquid chamber above the main body, and wherein the other end of the flow channel is connected to the loaded liquid chamber below the main body; and / or on the side wall of the pre-treatment chamber, a solvent inlet and a solvent outlet are provided, wherein the first tube extends into the pre-treatment chamber, and wherein the height of the air outlet end of the first tube in the vertical direction is greater than that of the solvent outlet; and / or the air outlet end of the first tube is provided with an air distribution cap.In some embodiments, it further comprises a second tube, wherein one end of the second tube is connected to the absorption chamber and the other end of the second tube is connected to the loaded liquid chamber, and wherein the absorption medium in the absorption chamber flows into the loaded liquid chamber through the second tube.In some embodiments, it further comprises a third pipe, wherein one end of the third pipe extends into the absorption chamber, and wherein the other end of the third pipe is connected to the pretreatment chamber, and wherein the height of an end of the third pipe extending into the absorption chamber in the vertical direction is greater than the height of an end of the second pipe connected to the absorption chamber, and wherein the flue gas in the pretreatment chamber flows into the absorption chamber through the third pipe.In some embodiments, the second tube and the third tube are disposed in the tower body; and / or the tower body comprises a first segment, a second segment, and a third segment, wherein the absorption chamber is disposed in the first segment, the pretreatment chamber is disposed in the second segment, and the loaded liquid chamber is disposed in the third segment, and wherein the first segment, the second segment, and the third segment are connected by bolts; and / or an end of the third tube extending into the absorption chamber is connected to an air distribution cap.In some embodiments, the carbon separation and absorption tower further comprises a de-nebulizer disposed at the tip portion of the absorption chamber, and wherein the flue gas is discharged from the flue gas outlet after having passed the de-nebulizer after removing carbon dioxide; and / or the carbon separation and absorption tower further comprises a liquid distributor, wherein a liquid distributor is disposed in each of the pre-treatment chamber and the absorption chamber; and / or a magnesium oxide solvent is introduced into the pre-treatment chamber to desulfurize the flue gas.The carbon separation and absorption tower of the present invention, by integrating the pretreatment unit and the heat exchange unit of flue gas into the tower body, improves the degree of integration of the plant, reduces the space requirement, and enables heat exchange of the flue gas with the absorption medium in the loaded liquid chamber inside the tower body, reduces the reaction temperature between the flue gas and the absorption medium in the absorption chamber, and at the same time, increases the temperature of the carbon dioxide-absorbed absorption medium flowing out of the tower body, and improves the efficiency of utilization of the flue gas heat and the absorption efficiency of carbon separation.BRIEF DESCRIPTION OF THE DRAWINGSFIG. 1 is a schematic diagram of the structure, a tower for depositing and absorbing carbon according to an embodiment of the present invention. FIG. 2 is a schematic diagram of the structure, a tower for depositing and absorbing carbon according to another embodiment of the present invention.List of reference characters100 Tower for separating and absorbing carbon 1 Tower body 11 Absorption chamber 12 Pretreatment chamber 121 Solvent inlet 122 Solvent outlet 13 Loaded liquid chamber 14 Medium inlet 15 Flue gas outlet 16 Medium outlet 17 Flue gas inlet 2 First heat exchanger component 21 Base body 22 First tube 221 Air distribution cap 23 Throughflow gap 24 Throughflow channel 3 Second heat exchanger component 4 Filling layer 5 Second tube 6 Third tube 7 Liquid distributor 8 DenebelerDETAILED DESCRIPTIONThe embodiments of the present invention will be explained in more detail below, and the examples of the embodiments are illustrated in the accompanying drawings. The embodiments explained in connection with the attached drawings are exemplary, serve only to explain the present invention and cannot be understood as limiting the present invention.Referring to FIGS. 1 and 2, a carbon separation and absorption tower 100 according to an embodiment of the present invention includes a tower body 1, a first heat exchange component 2, and a second heat exchange component 3.The tower body 1 has an absorption chamber 11, a pretreatment chamber 12, and a loaded liquid chamber 13, wherein a medium inlet 14 and a flue gas outlet 15 are provided at the tip portion of the tower body 1, and wherein a medium outlet 16 and a flue gas inlet 17 are provided at the bottom portion of the tower body 1; it should be understood that, in order to reverse the flow of the flue gas and the absorption medium and to improve the effect of carbon deposition, the absorption chamber 11, the pretreatment chamber 12, and the loaded liquid chamber 13 in the embodiment of the present invention are sequentially set in the tower body 1 from top to bottom in the height direction. The flue gas enters the tower body 1 through the flue gas inlet 17 and is discharged from the flue gas outlet 15, the absorption medium enters the tower body 1 through the medium inlet 14 and is discharged from the medium outlet 16, wherein the absorption medium, also referred to as separation solution, is used to perform an absorption reaction with carbon dioxide in the flue gas.In the embodiment of the present invention, the first heat exchanger component 2 is arranged in the loaded liquid chamber 13, wherein the flue gas inlet 17 is connected to the first heat exchanger component 2 to allow the flue gas entering the first heat exchanger component 2 to exchange heat with an absorption medium in the loaded liquid chamber 13, and wherein the cooled flue gas enters the absorption chamber 11 after passing through the pretreatment chamber 12, and wherein the heated absorption medium is discharged through the medium outlet 16; the second heat exchanger component 3 is arranged in the absorption chamber 11, wherein the medium inlet 14 is connected to the absorption chamber 11, and wherein the second heat exchanger component 3 is used to cool the absorption medium and / or the flue gas in the absorption chamber 11, and wherein the flue gas is discharged via the flue gas outlet 15 after the removal of carbon dioxide and the absorption medium flows into the loaded liquid chamber 13 after the absorption of carbon dioxide.In particular, the temperature of the flue gas is high when it enters the first heat exchange component 2, and when it is directly fed into the absorption chamber 11, it causes the reaction temperature with the absorption medium to be too high, which is unfavorable for the absorption of carbon dioxide, and in the embodiment of the present invention, by the indirect contact of the flue gas with the absorption medium in the loaded liquid chamber 13 for heat exchange, it is possible to lower the temperature of the flue gas and simultaneously raise the temperature of the absorption medium in the loaded liquid chamber 13. Since the absorption medium in the loaded liquid chamber 13 is the absorption medium after absorption of carbon dioxide, which is also referred to as rich liquid, raising the temperature of the rich liquid for desorption of carbon dioxide from the rich liquid in the following process is favorable and reduces power consumption during desorption.In the embodiment of the present invention, the flue gas after heat exchange with the rich liquid flows into the pretreatment chamber 12, the flue gas comes into contact with the pretreatment solvent in the pretreatment chamber 12, and desulfurization, denitrification, and other treatments are performed on the flue gas, at which time the temperature of the flue gas can be further lowered, and the flue gas finally flows into the absorption chamber 11 and flows from bottom to top, and the absorption medium flows from bottom to top after entering the absorption chamber 11, and the flue gas undergoes an absorption reaction after coming into contact with the absorption medium, whereby carbon dioxide is absorbed in the flue gas, the flue gas after removing carbon dioxide is discharged from the flue gas outlet 15, and the absorption medium that has absorbed the carbon dioxide, The liquid enters the loaded liquid chamber 13 and absorbs the heat, and is then discharged from the medium outlet 16.The second heat exchange component 3 is disposed in the absorption chamber 11 capable of cooling the flue gas and the absorption medium passing through the second heat exchange component 3 to control the temperature of the flue gas and the absorption medium when the absorption reaction takes place, thereby preventing the temperature from being too high and impairing the absorption efficiency.In some embodiments, the carbon deposition and absorption tower 100 further comprises a filling layer 4 arranged in the absorption chamber 11, wherein the filling layer 4 is arranged below the second heat exchanger component 3. It should be understood that the filling layer 4 can make complete contact between the flue gas and the absorption medium and increase the contact time to provide sufficient time for the absorption reaction of the two and improve the absorption efficiency, and by disposing the filling layer 4 below the second heat exchange component 3, the absorption medium can be allowed to enter the filling layer 4 after cooling to more realize the adjustment of the reaction temperature.In some embodiments, the second heat exchanger components 3 and the filling layers 4 are each provided in a number of more than 1, wherein the plurality of second heat exchanger components 3 are arranged at intervals along the flow direction of the absorption medium, and wherein the plurality of filling layers 4 are arranged at intervals along the flow direction of the absorption medium; and wherein the filling layers 4 and the second heat exchanger components 3 are arranged one-to-one, respectively, and wherein the filling layer 4 is arranged below the corresponding second heat exchanger component 3.In other words, by disposing a plurality of filling layers 4 and a plurality of second heat exchanger components 3, the reaction time and the reaction temperature of the flue gas and the absorption medium can be more controlled, and a single filling layer 4 can be prevented from being too thick, resulting in that the heat released between the absorption medium and the flue gas during the absorption reaction cannot be discharged in time and thus the absorption efficiency is impaired.By disposing a plurality of filling layers 4 and a plurality of second heat exchange components 3 in the embodiment of the present invention, the reaction temperature in each of the filling layers 4 can be controlled to be in the optimum temperature interval, which promotes the progress of the absorption reaction and improves the deposition efficiency.For example, when two filling layers 4 and two second heat exchange components 3 are arranged, the temperature of the absorption medium entering the absorption chamber 11 from the medium inlet 14 is about 50° C. The temperature of the absorption medium is lowered to about 35° C. after the heat exchange by the above second heat exchange component 3, and the absorption medium flows into the above filling layer 4 and has an exothermic chemical reaction with the carbon dioxide in the flue gas in the flue gas 4, and the filling layer 4 can extend the gas-liquid contact time to improve the absorption efficiency of the carbon dioxide; the absorption medium flowing out of the upper filling layer 4 is a semi-clean liquid, the temperature of the semi-clean liquid rises (may rise to about 60° C. or higher) as the temperature further rises, it will not be conducive to the progress of the chemical reaction, at which time the semi-clean liquid is cooled by the lower second heat exchange component 3, after cooling, the temperature is controlled to about 40° C., so that the semi-clean liquid can flow into the next filling layer 4 to further absorb the carbon dioxide.A further example is the arrangement of three filling layers 4 and three second heat exchanger components 3 which functions in the same way as in the previous example, wherein the number of filling layers 4 and second heat exchanger components 3 can be adapted to the height of the absorption chamber 11.The second heat exchanger component 3 is not only capable of cooling the absorption medium entering the underlying filling layer 4, but at the same time also of cooling the flue gas flowing through the second heat exchanger component 3.In some embodiments, the carbon deposition and absorption tower 100 further comprises a temperature sensing component and a control component, wherein the temperature sensing component is used to sense the temperature of the absorption medium flowing into the filling layer 4, and wherein the control component is connected to the second heat exchange component 3, and wherein the control component is used to control the flow rate of the heat exchange medium in the second heat exchange component 3 such that the temperature of the absorption medium entering the filling layer 4 is less than a first threshold.The embodiment of the present invention may detect the temperature of the absorption medium in real time by arranging the temperature detection component to prevent the temperature of the absorption medium from being too high, and the control component may control the flow rate of the heat exchange medium in the second heat exchange component 3 according to the temperature information detected by the temperature detection component, so that when the temperature of the absorption medium is too high and the heat exchange medium at the current flow rate is unable to cool the absorption medium to the first threshold value, the flow rate of the heat exchange medium may be increased to improve the cooling effect on the heat exchange medium.The first threshold may be 30° C., 35° C., 36° C., 36.5° C., 38.3° C., 42° C., or 45° C. The magnitude of the first threshold is determined according to the optimum reaction temperature interval between the separation solution and the carbon dioxide to improve the absorption efficiency.Optionally, the heat exchange medium in the second heat exchange component 3 is cooling water from a power plant, and the temperature of the cooling water supplied into the second heat exchange component 3 can also be controlled by the arrangement of a cooling system and the cooling of the cooling water with the cooling system, in order to conveniently ensure the cooling effect on the absorption medium and the flue gas inside the absorption chamber 11 in the case of a higher temperature in summer.In some embodiments, the first heat exchanger component 2 comprises a base body 21 and a plurality of first tubes 22, wherein the base body 21 has a first chamber, and wherein the flue gas inlet 17 is connected to the first chamber, and wherein the base body 21 is arranged in the chamber of the rich liquid 13, and wherein one end of the first tube 22 is connected to the first chamber and the other end of the first tube 22 is connected to the pretreatment chamber 12.It should be understood that the flue gas first enters the first chamber and then flows into the pretreatment chamber 12 through a plurality of first tubes 22, in this process, the flue gas can be equalized by means of the main body 21 and the first tubes 22, thereby improving the uniformity of distribution of the flue gas after flowing into the pretreatment chamber 12, improving the contact effect of the flue gas with the treatment solvent in the pretreatment chamber 12, improving the pretreatment effect of the flue gas, and improving the heat exchange effect of the flue gas with the absorbent in the chamber of the loaded liquid chamber 13, so that the flue gas and the absorbent in the chamber of the loaded liquid chamber 13 completely exchange heat indirectly.In some embodiments, the plurality of first tubes 22 are distributed in an array and at intervals in the loaded liquid chamber 13. In other words, the plurality of first tubes 22 are arranged in a rectangular arrangement or a circular arrangement in the loaded liquid chamber 13, adjacent first tubes 22 are spaced apart from each other, and the plurality of first tubes 22 are uniformly arranged in the loaded liquid chamber 13 to better ensure that the rich liquid can completely exchange heat with the flue gas at different locations in the loaded liquid chamber 13, thereby improving the efficiency of heat exchange.Further, the first heat exchanger component 2 further comprises a plurality of baffles, the plurality of baffles being distributed in the first chamber to disperse and deflect the flue gas entering the first chamber through the flue gas inlet 17. The baffles are disposed in the first chamber to disperse and deflect the flue gas entering the first chamber such that the flue gas can spread more evenly in the different areas of the first chamber and the flue gas flow in the plurality of first tubes 22 is relatively uniform and consistent to improve the heat exchange effect and avoid the presence of a dead corner of the flow.Further, the flue gas inlets 17 are provided in a number of more than 1, the plurality of flue gas inlets 17 being spaced along the circumferential direction of the main body 21. By disposing the plurality of flue gas inlets 17, the flue gas can enter the first chamber from a plurality of directions, thereby improving uniformity of distribution of the flue gas in the first chamber, and heat exchange effect and uniformity of distribution of the flue gas can be further improved.Optionally, a flow gap 23 is formed between the circumferential side wall of the base body 21 and the inner wall of the loaded liquid chamber 13. It should be understood that the first heat exchanger component 2 is disposed in the loaded liquid chamber 13 and does not influence the flow of the rich liquid, so that by forming the flow gap 23 between the circumferential side wall of the main body 21 and the inner wall of the loaded liquid chamber 13, the rich liquid 21 located above the main body 21 can be caused to perform the heat exchange again when flowing through the flow gap 23, and at the same time, the rich liquid is mixed above the main body 21 so that the temperature of the rich liquid flowing below the main body 21 is uniform.Optionally, the central part of the base body 21 has a flow channel 24, wherein one end of the flow channel 24 is connected to the loaded liquid chamber 13 above the base body 21, and wherein the other end of the flow channel 24 is connected to the loaded liquid chamber 13 below the base body 21. With the same purpose of providing the flow gap 23, the flow channel 24 may mix the rich liquid above the main body 21 and indirectly perform heat exchange with the flue gas in the first chamber when the rich liquid flows through the flow channel 24.The structural configuration of the base body 21 and the first pipe 22 of the embodiment of the present invention can improve the temperature consistency of the rich liquid discharged from the medium outlet 16, and can also make the flow of the flue gas uniform to improve the heat exchange effect, which also facilitates subsequent pretreatment of the flue gas and carbon deposition and improves the performance and integration of the absorption tower.In some embodiments, a solvent inlet 121 and a solvent outlet 122 are provided on the side wall of the pretreatment chamber 12, the first pipe 22 extends into the pretreatment chamber 12, and the height of the air outlet end of the first pipe 22 in the vertical direction is greater than that of the solvent outlet 122. In order to prevent the treatment solvent in the pretreatment chamber 12 from entering the first pipe 22, the height of the air outlet end of the first pipe 22 is set to be higher than the height of the solvent outlet 122, then the treatment solvent in the pretreatment chamber 12 can be discharged from the solvent outlet 122 in time.Optionally, the air outlet end of the first pipe 22 is provided with an air distribution cap 221. Thus, the sprayed treatment solvent can be prevented from entering the first pipe 22, and at the same time, the air distribution cap 221 can diffuse the flue gas exiting from the first pipe 22 to improve the uniformity of the flue gas in the pretreatment chamber 12.The air distribution cap 221 is formed in a taper shape, and a gap is provided between the air distribution cap 221 and the first pipe 22 to facilitate the flue gas to be discharged from the first pipe 22 and then diffused through the edge of the air distribution cap 221.Optionally, a magnesium oxide solvent is introduced into the pretreatment chamber 12 to desulfurize the flue gas. It can be ensured that desulfurization does not introduce new impurity gases into the entire carbon separation and absorption tower 100, and magnesium sulfite trihydrate and polyhydrate are mainly generated, and magnesium sulfate is generated in a stable and dissolved state by oxidation with oxygen in the flue gas, which has a high economic value.The magnesium oxide wet desulfurization technology can simultaneously bind H 2 O in the flue gas, reduce the dilution effect of H 2 O on the solvent for carbon deposition (absorption cut-off), and ensure the quality of the solvent without impairing the absorption efficiency.In some embodiments, the carbon separation and absorption tower 100 further comprises a second tube 5, wherein one end of the second tube 5 is connected to the absorption chamber 11 and the other end of the second tube 5 is connected to the loaded liquid chamber 13, and wherein the absorption medium in the absorption chamber 11 flows into the loaded liquid chamber 13 through the second tube 5.With the arrangement of the second tube 5, since the pretreatment chamber 12 is located between the absorption chamber 11 and the loaded liquid chamber 13, the absorption medium that has absorbed the carbon dioxide in the absorption chamber 11 can flow into the loaded liquid chamber 13 after passing through the second tube 5.In some embodiments, the carbon separation and absorption tower 100 further includes a third pipe 6, wherein one end of the third pipe 6 extends into the absorption chamber 11, and wherein the other end of the third pipe 6 is connected to the pretreatment chamber 12, and wherein the height of an end of the third pipe 6 extending into the absorption chamber 11 in the vertical direction is greater than the height of an end of the second pipe 5 connected to the absorption chamber 11, and wherein the flue gas in the pretreatment chamber 12 flows into the absorption chamber 11 through the third pipe 6. Since the bottom portion of the absorption chamber 11 contains an absorption medium, the third pipe 6 is arranged so that the flue gas in the pretreatment chamber 12 enters the absorption chamber 11 while preventing the absorption medium from flowing into the pretreatment chamber 12 via the third pipe 6.An end of the third tube 6 extending into the absorption chamber 11 is connected to an air distribution cap 221. Thus, it can be prevented that the absorption medium dripping from the filling layer 4 penetrates into the third pipe 6, and at the same time, the air distribution cap 221 can diffuse the flue gas exiting from the third pipe 6 to improve the uniformity of the flue gas in the pretreatment chamber 12.The air distribution cap 221 is formed in a taper shape, and a gap is provided between the air distribution cap 221 and the third pipe 6 to facilitate the flue gas to be discharged from the third pipe 6 and then diffused through the edge of the air distribution cap 221.In some embodiments, the second tube 5 and the third tube 6 are arranged in the tower body 1. It is understood that the present invention avoids the external piping of the tower body 1 by integrating the second pipe 5 and the third pipe 6 into the tower body 1 and also enables better control of the flow of liquids and gases, thereby achieving a higher degree of integration.In some embodiments, the tower body 1 comprises a first segment, a second segment and a third segment, wherein the absorption chamber 11 is arranged in the first segment, the pretreatment chamber 12 is arranged in the second segment and the loaded liquid chamber 13 is arranged in the third segment, and wherein the first segment, the second segment and the third segment are connected by bolts. By dividing the tower body 1 into segments, the materials and properties of the various segments can be selected better, e.g. the materials in the pretreatment chamber 12 can be selected according to the corrosion resistance in order to improve the service life of the corresponding segments. Expansion joints can be provided between two adjacent segments in order to avoid leaks when connecting segments made of different materials.In some embodiments, the carbon separation and absorption tower 100 further includes a deneubler 8 disposed at the tip portion of the absorption chamber 11, and the flue gas after removing carbon dioxide is discharged from the flue gas outlet 15 after passing through the deneubler 8. The deneubler 8 is arranged between the medium inlet 14 and the flue gas outlet 15, the medium inlet 14 is arranged below the deneubler 8, and the flue gas outlet 15 is arranged above the deneubler 8, so that when the flue gas from which the carbon dioxide has been extracted passes the deneubler 8, the liquid in the interior can be removed and thus the net flue gas is discharged.The carbon separation and absorption tower 100 further comprises a liquid distributor 7, wherein a liquid distributor 7 is arranged in each of the pretreatment chamber 12 and the absorption chamber 11. The liquid distributor 7 allows the absorption medium and the treatment solvent to be more uniformly sprayed into the corresponding absorption chamber 11 or the pretreatment chamber 12, and the liquid distributor 7 includes a liquid distribution pipe and a nozzle so that the absorption medium is sprayed through the liquid distribution pipe and the nozzle after having entered the absorption chamber 11, and can be more uniformly distributed in the filling layer 4, thereby improving the reaction effect with the flue gas, and avoiding the uneven distribution of the absorption medium in the filling layer 4 that causes the carbon dioxide in the flue gas to be unable to be efficiently absorbed in some areas.The present invention can be achieved by disposing a plurality of filling layers 4 that divide the inside of the absorption chamber 11 into a plurality of mixing spaces on the upper and lower sides of the filling layers 4, mixing the flue gas in the mixing spaces, and then entering the upper-level filling layer 4 to improve uniformity of distribution of the flue gas and improve the reaction effect of the flue gas and the absorbent. The carbon separation and absorption tower of the present invention, by integrating the pretreatment unit and the heat exchange unit of flue gas into the tower body, improves the degree of integration of the plant, reduces the space requirement, and enables heat exchange of the flue gas with the absorption medium in the rich liquid chamber inside the tower body, reduces the reaction temperature between the flue gas and the absorption medium in the absorption chamber, and at the same time, increases the temperature of the carbon dioxide-absorbed absorption medium flowing out of the tower body, and improves the efficiency of utilization of the flue gas heat and the absorption efficiency of carbon separation.The invention utilizes flue gas discharged from the chimney of the power plant for the primary heat exchange of the rich liquid, thereby reducing the subsequent heat consumption of the reboiler and hence the heat consumption of the system; the combination of desulfurization, cooling and absorption in a tower effectively reduces the space requirement of the carbon deposition system, so that it is more suitable for the newly added carbon deposition apparatus in the existing power plant; by the omission of the intermediate cooling tanks, the heat exchange and cooling unit of the medium-lean liquid is integrated into the absorption tower, whereby the absorption efficiency can be effectively improved to reduce the solvent requirement of the system and thus reduce the running costs; The temperature of the flue gas after desulfurization by magnesium oxide is about 50°C, which is within the optimum temperature interval of the chemical absorption reaction, and there is no need to separately cool the flue gas to meet the reaction conditions, and the power consumption of the cooling water system can be effectively reduced; the present invention can also replace the solvent of the desulfurization unit with other solvents to adapt to the pretreatment situation of various flue gas components.It should be noted that, in the explanation of the present invention, the directional or positional relationships with the terms such as "center", "longitudinal", "quee", "length", "width", "thickness", "top", "bottom", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. are based on the directional or positional relationships illustrated in the figures. They are for the purpose of illustrating the present invention and facilitating the explanation only and do not indicate and suggest that the devices or elements illustrated have certain directions or should be constructed and operated in certain directions. Therefore, they cannot be understood as being a limitation to the present invention.Moreover, "the first," "the second" are used only to explain the goal, and they cannot be understood to instruct or imply the relative meaning or to implicitly indicate the number of technical features instructed. Due to this, the features defined with "the first", "the second" may include at least one of the features explicitly or implicitly. In the explanation of the present invention, "plural" refers to at least 2, such as 2, 3, etc., unless otherwise specified.Unless otherwise expressly stated and defined in the present invention, the terms "installation", "coupling", "connection" and "attachment" should be understood in the broader sense, e.g., the "attachment" may be both a fixed connection and a detachable connection, or an integrated connection; it may be a mechanical connection or an electrical connection or mutual communication; it may be a direct connection or a connection via a medium; it may also be a connection within two elements or an interaction relationship between two elements, unless otherwise specified. Those skilled in the art can understand the concrete meanings of the above technical words in the present invention from the concrete situations.In the present invention, the phrase that the first feature is "above" or "below" the second feature may refer to the first feature and the second feature being in direct contact or the first feature and the second feature being in indirect contact through an intermediate medium, unless there are other unique findings and definitions. Moreover, the phrase that the first feature is "above the second feature", "above the second feature", or "at the top of the second feature" may refer to the first feature being directly above or obliquely above the second feature, or the horizontal height of the first feature being greater than that of the second feature. Moreover, the phrase that the first feature is "below the second feature", "below the second feature", or "at the bottom of the second feature" may refer to the first feature being directly below or obliquely below the second feature, or the horizontal height of the first feature being less than that of the second feature.In the present invention, the words of language "an embodiment," "some embodiments," "an example," "a specific example," or "some examples" refer to the specific features, structures, materials, or features discussed in connection with the embodiment or example being included in at least one embodiment or example of the present invention. In the present specification, the schematic diagrams of the above technical words do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials, or features discussed may be combined as appropriate in one or more embodiments or examples. In the event of no conflicts, those skilled in the art may additionally connect and combine various embodiments or examples discussed in this specification or the features in the various embodiments or examples.Although the embodiments of the present invention are illustrated and explained above, it is to be understood that the above embodiments are exemplary and should not be taken as limiting the present invention. Those skilled in the art can make the changes, modifications, substitutions, and variations for the embodiments within the scope of the present invention.

Claims

A tower for separating and absorbing carbon, characterized by comprising: a tower body having an absorption chamber, a pretreatment chamber and a loaded liquid chamber, wherein a medium inlet and a flue gas outlet are provided at the tip portion of the tower body, and wherein a medium outlet and a flue gas inlet are provided at the bottom portion of the tower body; a first heat exchange component disposed in the loaded liquid chamber, wherein the flue gas inlet is connected to the first heat exchange component to allow the flue gas entering the first heat exchange component to exchange heat with an absorption medium in the loaded liquid chamber, and wherein the cooled flue gas enters the absorption chamber after passing through the pretreatment chamber, and wherein the heated absorption medium is discharged through the medium outlet; a second heat exchanger component arranged in the absorption chamber, wherein the medium inlet is connected to the absorption chamber, and wherein the second heat exchanger component is used to cool the absorption medium and / or the flue gas in the absorption chamber, and wherein the flue gas is discharged via the flue gas outlet after removal of carbon dioxide and the absorption medium flows into the loaded liquid chamber after absorption of carbon dioxide.The carbon deposition and absorption tower according to claim 1, characterized in that it further comprises a filling layer arranged in the absorption chamber, said filling layer being arranged below the second heat exchanger component.The carbon deposition and absorption tower according to claim 2, characterized in that the number of the second heat exchange components and the filling layers are each a plurality, wherein the plurality of the second heat exchange components are spaced apart along the flow direction of the absorption medium, and wherein the plurality of the filling layer are spaced apart along the flow direction of the absorption medium; and wherein the filling layers and the second heat exchange components are disposed one-to-one, respectively, and wherein the filling layer is disposed below the corresponding second heat exchange component.The carbon deposition and absorption tower according to claim 3, characterized in that it further comprises a temperature sensing component and a control component, wherein the temperature sensing component is used to sense the temperature of the absorption medium flowing into the filling layer, and wherein the control component is connected to the second heat exchange component, and wherein the control component is used to control the flow rate of the heat exchange medium in the second heat exchange component such that the temperature of the absorption medium entering the filling layer is less than a first threshold value.The carbon separation and absorption tower of claim 1, characterized in that the first heat exchanger component comprises a base body and a plurality of first tubes, wherein the base body has a first chamber, and wherein the flue gas inlet is connected to the first chamber, and wherein the base body is arranged in the loaded liquid chamber, and wherein one end of the first tube is connected to the first chamber and the other end of the first tube is connected to the pretreatment chamber.The carbon separation and absorption tower of claim 5, characterized in that the plurality of first tubes are in an array and spaced apart in the loaded liquid chamber; and / or the first heat exchanger component further comprises a plurality of baffles, the plurality of baffles being spaced apart in the first chamber to disperse and deflect the flue gas entering the first chamber through the flue gas inlet; and / or the number of flue gas inlets is a plurality, the plurality of flue gas inlets being spaced apart along the circumferential direction of the base body; and / or a flow gap is formed between the circumferential sidewall of the base body and the inner wall of the loaded liquid chamber; and / or the central part of the main body has a flow channel, wherein one end of the flow channel is connected to the loaded liquid chamber above the main body, and wherein the other end of the flow channel is connected to the loaded liquid chamber below the main body; and / or a solvent inlet and a solvent outlet are provided on the side wall of the pre-treatment chamber, wherein the first tube extends into the pre-treatment chamber, and wherein the height of the air outlet end of the first tube in the vertical direction is greater than that of the solvent outlet; and / or the air outlet end of the first tube is provided with an air distribution cap.The carbon separation and absorption tower according to claim 1, characterized by further comprising a second pipe, wherein one end of the second pipe is connected to the absorption chamber and the other end of the second pipe is connected to the loaded liquid chamber, and wherein the absorption medium in the absorption chamber flows into the loaded liquid chamber through the second pipe.The carbon separation and absorption tower according to claim 7, characterized by further comprising a third pipe, wherein one end of the third pipe extends into the absorption chamber, and wherein the other end of the third pipe is connected to the pretreatment chamber, and wherein the height of an end of the third pipe extending into the absorption chamber in the vertical direction is greater than the height of an end of the second pipe connected to the absorption chamber, and wherein the flue gas in the pretreatment chamber flows into the absorption chamber through the third pipe.The carbon separation and absorption tower of claim 8, characterized in that the second tube and the third tube are arranged in the tower body; and / or the tower body comprises a first segment, a second segment and a third segment, wherein the absorption chamber is arranged in the first segment, the pretreatment chamber is arranged in the second segment and the loaded liquid chamber is arranged in the third segment, and wherein the first segment, the second segment and the third segment are connected by bolts; and / or an end of the third tube extending into the absorption chamber is connected to an air distribution cap.The carbon separation and absorption tower according to claim 1, characterized in that it further comprises a de-nebulizer disposed at the tip portion of the absorption chamber, wherein the flue gas after removing carbon dioxide is discharged from the flue gas outlet after passing through the de-nebulizer; and / or it further comprises a liquid distributor, wherein a liquid distributor is disposed in each of the pre-treatment chamber and the absorption chamber; and / or a magnesium oxide solvent is introduced into the pre-treatment chamber to desulfurize the flue gas.

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