Highly integrated flue gas low-temperature adsorption regeneration system

Abstract

The present application relates to the technical field of adsorption purification, and discloses a highly integrated flue gas low-temperature adsorption regeneration system. The system comprises an adsorbent circulation treatment tower and an adsorption tower; an inner cavity of the adsorbent circulation treatment tower is divided into a regeneration section, a pre-cooling section and a low-temperature cooling section which are sequentially arranged in an up-down direction; a feeding loop is provided between a feeding port of the adsorption tower and a discharging port of the adsorbent circulation treatment tower; and a discharging loop is provided between a discharging port of the adsorption tower and a feeding port of the adsorbent circulation treatment tower. In the highly integrated flue gas low-temperature adsorption regeneration system of the present application, a spray cooling tower and connecting pipelines between the spray cooling tower and the adsorption tower and the adsorbent circulation treatment tower do not need to be additionally provided, thereby reducing the number of system devices and connecting pipelines, simplifying the whole system, simplifying the working procedures, reducing the occupied area, improving the integration degree of the system, reducing the cost, and improving the flue gas treatment efficiency.

Description

Highly integrated flue gas low-temperature adsorption regeneration system

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] This application is based on the Chinese patent application number 202410250442.5 and the application date of March 5, 2024, and claims the priority of the Chinese patent application. The entire content of the Chinese patent application is hereby introduced into this application as a reference. Technical Field

[0003] The present application relates to the field of adsorption purification technology, and in particular to a highly integrated flue gas low-temperature adsorption regeneration system. Background Art

[0004] The flue gas from a coal-fired boiler is generally desulfurized and denitrified by passing through an adsorption tower and a regeneration tower. Specifically, the flue gas discharged from the coal-fired boiler enters the adsorption tower, and the pollutants (sulfides and nitrogen compounds) in the flue gas are absorbed by the adsorbent in the adsorption tower. The adsorbent to be regenerated (adsorbent to be regenerated) that has adsorbed the pollutants in the flue gas is transported to the heating section of the regeneration tower for heating, desorption and regeneration. The sulfides and nitrogen compounds are desorbed from the adsorbent and recycled. The desorbed and regenerated adsorbent is returned to the adsorption tower for continued adsorption and purification of the sulfides and nitrogen compounds in the flue gas. Therefore, the adsorbent is circulated between the adsorption tower and the regeneration tower to continuously remove the sulfides and nitrogen compounds in the flue gas.

[0005] Traditionally, the adsorbent is usually used to perform high-temperature adsorption on flue gas at 200°C in the adsorption tower. High-temperature adsorption leads to large adsorbent consumption, poor adsorption effect, and high nitrogen oxide content in the clean flue gas after adsorption. Summary of the Invention

[0006] This application is based on the inventor's discovery and understanding of the following facts and problems:

[0007] To overcome the problems of high-temperature adsorption, low-temperature adsorption has been proposed in related technologies. This involves adsorption and purification of flue gas at temperatures below room temperature. The high-temperature flue gas is first cooled to low-temperature flue gas in a spray cooling tower. The low-temperature flue gas is then fed into an adsorption tower for low-temperature adsorption. After adsorption saturation, the adsorbent to be regenerated is fed into a regeneration tower for heating and desorption regeneration. The regenerated adsorbent is then fed back into the adsorption tower. Cooling the flue gas to low-temperature flue gas requires the installation of flue gas cooling equipment, such as a spray cooling tower, before the adsorption tower. This results in a complex system with numerous devices, a large footprint, high energy consumption, and high costs.

[0008] In addition, the temperature of the desorbed and regenerated adsorbent discharged from the regeneration tower is relatively high (generally above 300°C), so the heat carried by the regenerated adsorbent is relatively large. For this reason, the relevant technology proposes to use ambient air to perform a preliminary cooling of the desorbed and regenerated adsorbent before supplying the adsorbent to the adsorption tower. Through research, the inventors discovered and realized that when the desorbed and regenerated adsorbent is initially cooled using ambient air, the temperature of the adsorbent is still relatively high, at least more than ten degrees Celsius higher than room temperature, or even dozens of degrees Celsius, which cannot meet the low-temperature adsorption requirements. It is still necessary to use waste gas cooling equipment such as spray cooling towers to cool the flue gas into low-temperature flue gas before the flue gas enters the adsorption tower for low-temperature adsorption. Not only can the above problems not be solved, but the need for equipment to agitate ambient air to cool the adsorbent further increases costs and energy consumption.

[0009] The present application aims to solve at least one of the technical problems in the related art to a certain extent. To this end, the embodiments of the present application propose a highly integrated flue gas low-temperature adsorption regeneration system with a simple system, low cost and energy consumption.

[0010] The highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application includes an adsorbent circulation treatment tower and an adsorption tower, the inner cavity of the adsorbent circulation treatment tower is divided into a regeneration section, a pre-cooling section and a low-temperature cooling section arranged in sequence along the up and down directions, the regeneration section is used to heat the adsorbent to be regenerated to a first temperature so that the adsorbent to be regenerated is desorbed and regenerated, the pre-cooling section is used to pre-cool the regenerated adsorbent from the regeneration section to a second temperature, and the low-temperature cooling section is used to further cool the pre-cooled adsorbent from the pre-cooling section to a third temperature to become a low-temperature adsorbent, wherein the first temperature is higher than the second temperature, the second temperature is higher than the third temperature, and the third temperature is below room temperature, the adsorbent circulation treatment tower has a feed port and a discharge port, the feed port is used to supply the adsorbent to be regenerated into the regeneration section, and the discharge port is used to discharge the low-temperature adsorbent from the low-temperature cooling section;

[0011] The adsorption tower has a feeding port and a discharging port. A feeding circuit is provided between the feeding port of the adsorption tower and the discharging port of the adsorbent circulation treatment tower, which is used to transport the low-temperature adsorbent discharged from the adsorbent circulation treatment tower into the adsorption tower so as to perform low-temperature adsorption purification on the flue gas in the adsorption tower. A discharging circuit is provided between the discharging port of the adsorption tower and the feeding port of the adsorbent circulation treatment tower, which is used to transport the adsorbent to be regenerated discharged from the adsorption tower into the adsorbent circulation treatment tower so as to heat the adsorbent to be regenerated in the adsorbent circulation treatment tower so as to desorb and regenerate it and cool the regenerated adsorbent into the low-temperature adsorbent.

[0012] The highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application can not only desorb and regenerate the adsorbent to be regenerated, but also pre-cool and low-temperature cool the adsorbent in the circulation treatment tower to below room temperature through the regeneration section, pre-cooling section and low-temperature cooling section arranged in sequence along the upper and lower directions in the adsorbent circulation treatment tower, so that the adsorbent circulation treatment tower integrates multiple functions of regeneration, pre-cooling and low-temperature cooling, thereby making the flue gas low-temperature adsorption regeneration system highly integrated.

[0013] Moreover, the adsorbent to be regenerated in the adsorption tower is input into the adsorbent circulation treatment tower through the discharge loop for desorption and cooling to below room temperature. The low-temperature adsorbent after desorption and regeneration can be directly returned to the adsorption tower through the feeding loop for low-temperature adsorption of the flue gas, thereby realizing low-temperature adsorption and desorption regeneration of the adsorbent between the adsorption tower and the adsorbent circulation treatment tower. In other words, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application can no longer be separately provided with a spray cooling tower device for cooling the flue gas to low-temperature flue gas and then sending it to the adsorption tower for low-temperature adsorption, as well as the connecting pipelines between the spray cooling tower and the adsorption tower and the adsorbent circulation treatment tower, thereby reducing the number of system equipment and connecting pipelines, making the system simple, simplifying the process, reducing the floor space, improving the integration of the system, reducing costs, and improving the flue gas treatment efficiency.

[0014] Therefore, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application has the advantages of simple system, simplified process, small occupied area, high integration, high flue gas treatment efficiency and low cost.

[0015] In some embodiments, in the regeneration section, the adsorbent to be regenerated is subjected to indirect heat exchange with the first heat exchange medium to heat the adsorbent to be regenerated for desorption and regeneration, thereby avoiding direct contact between the adsorbent and the first heat exchange medium, which would affect the desorption effect of the adsorbent, thereby facilitating improvement of the desorption efficiency of the adsorbent; and / or

[0016] In the pre-cooling section, the regenerated adsorbent is subjected to indirect heat exchange with the second heat exchange medium to pre-cool the regenerated adsorbent. By indirect heat exchange between the adsorbent and the second heat exchange medium in the pre-cooling section, the adsorbent is further desorbed in the early stage of the pre-cooling section, which is further conducive to improving the desorption efficiency of the adsorbent; and / or

[0017] In the low-temperature cooling section, the pre-cooled adsorbent is in direct contact with the third heat exchange medium for heat exchange, so as to further cool the adsorbent to form the low-temperature adsorbent, which is beneficial to improving the heat exchange efficiency and further improving the cooling effect on the adsorbent.

[0018] In some embodiments, the first heat exchange medium is high-temperature air having a temperature higher than the first temperature, the second heat exchange medium is room-temperature air, and the third heat exchange medium is low-temperature air having a temperature not higher than the third temperature.

[0019] In some embodiments, the first temperature is not less than 300° C., and the desorption rate of the adsorbent to be regenerated is positively correlated with the heating temperature. That is, the higher the temperature at which the adsorbent is heated, the higher the desorption efficiency of the adsorbent. However, correspondingly, the higher the temperature at which the adsorbent is heated, the higher the cost. Therefore, the first temperature can be reasonably set according to the requirements of the desorption efficiency of different adsorbents to balance the desorption efficiency and cost of the adsorbent; and / or

[0020] The second temperature is 30°C to 150°C. If the second temperature is set too high, the difference between the second temperature and the first temperature is small, and the difference between the second temperature and the third temperature is large, which will weaken the effect of step-by-step cooling of the adsorbent (pre-cooling first, then low-temperature cooling); if the second temperature is set too low, the difference between the second temperature and the first temperature is large, and the difference between the second temperature and the third temperature is small, which will also weaken the effect of step-by-step cooling of the adsorbent; and / or

[0021] The third temperature is between -80°C and -5°C. The adsorption efficiency of the adsorbent is positively correlated with its temperature. That is, the lower the adsorbent temperature, the higher the adsorption efficiency. However, if the adsorbent temperature is set too low, the corresponding heat exchange medium temperature will also be too low, and the production cost of the heat exchange medium with a lower temperature will be higher. Therefore, the third temperature can be reasonably set according to the adsorption efficiency requirements of different adsorbents, taking into account both the adsorption efficiency and cost of the adsorbent.

[0022] In some embodiments, a first pipeline is provided between the pre-cooling section and the low-temperature cooling section for conveying the third heat exchange medium discharged from the low-temperature cooling section after heat exchange to the pre-cooling section. In other words, the heat exchange medium in the low-temperature cooling section and the pre-cooling section is the same heat exchange medium, but at different temperatures. Thus, only one heat exchange medium is required to achieve step-by-step cooling of the adsorbent, fully utilizing the heat exchange medium and avoiding the need for a separate heat exchange medium to cool the adsorbent in the pre-cooling section. This significantly reduces the manufacturing cost of the heat exchange medium, improving the utilization rate of the heat exchange medium and saving costs.

[0023] In some embodiments, the adsorbent circulation treatment tower of the embodiment of the present application further includes a heater, and a second pipeline is provided between the heater and the pre-cooling section for conveying the second heat exchange medium after heat exchange in the pre-cooling section to the heater, and a third pipeline is provided between the heater and the regeneration section, and the heater heats the second heat exchange medium after heat exchange and conveys it to the regeneration section as the first heat exchange medium through the third pipeline. The adsorbent circulation treatment tower of the embodiment of the present application heats the second heat exchange medium and inputs it into the regeneration section as the first heat exchange medium by providing a heater. In other words, through the provision of the heater, the same heat exchange medium can be used in the pre-cooling section and the regeneration section, and the temperatures of the heat exchange medium in the two sections are different, thereby achieving full utilization of the heat exchange medium and avoiding the need to separately provide another heat exchange medium to cool the adsorbent in the pre-cooling section, thereby greatly reducing the manufacturing cost of the heat exchange medium, which not only improves the utilization rate of the heat exchange medium but also saves costs.

[0024] In some embodiments, the inner cavity of the adsorbent circulation treatment tower further has a preheating section located above the regeneration section, and the first heat exchange medium discharged from the regeneration section after heat exchange enters the preheating section through a fourth pipeline to preheat the adsorbent. The first heat exchange medium enters the preheating section through the fourth pipeline to preheat the adsorbent in the preheating section, thereby realizing the recovery and utilization of the residual heat after heat exchange of the first heat exchange medium and preventing the waste of the residual heat after heat exchange of the first heat exchange medium. In addition, the adsorbent circulation treatment tower of the embodiment of the present application is preheated by the adsorbent, which is beneficial to the rapid desorption and regeneration of the adsorbent in the regeneration section, thereby helping to improve the regeneration efficiency of the adsorbent.

[0025] In some embodiments, the inner cavity of the adsorbent circulation treatment tower further has a buffer section, and the buffer section is provided between the regeneration section and the pre-cooling section. The adsorbent circulation treatment tower of the embodiment of the present application sets a buffer section between the regeneration section and the pre-cooling section, and the adsorbent flowing out of the regeneration section can play a buffering role in the buffer section, so that the adsorbent can smoothly flow downward to the low-temperature cooling section, and it is convenient for the adsorbent to be separated from the desorbed rich gas. In addition, due to the different temperatures between the regeneration section and the pre-cooling section, the regeneration section requires a first heat exchange medium with a higher temperature for adsorbent desorption and regeneration, and the pre-cooling section requires a second heat exchange medium with a lower temperature for cooling the adsorbent. The adsorbent in the buffer section can isolate the regeneration section from the low-temperature cooling section to prevent the temperatures between the regeneration section and the pre-cooling section from affecting each other, which is beneficial to improving the working reliability of the regeneration section and the pre-cooling section.

[0026] In some embodiments, a plurality of first discharge pipes and a plurality of first baffles are provided in the regeneration section, and the plurality of first baffles are arranged at intervals in the regeneration section to form a first serpentine channel for the circulation of the first heat exchange medium, and the first discharge pipe passes through at least a portion of the first baffles along the arrangement direction of the first baffles, and the adsorbent desorbed and regenerated in the regeneration section enters the pre-cooling section through the first discharge pipe; by arranging a plurality of first baffles in the regeneration section to form a first serpentine channel, the path of the first heat exchange medium in the regeneration section can be increased, so as to increase the residence time of the first heat exchange medium in the regeneration section, thereby allowing the first heat exchange medium and the adsorbent to fully exchange heat, so that the sulfide and nitride can be quickly dissociated from the adsorbent, which is beneficial to improving the desorption and regeneration efficiency of the adsorbent.

[0027] In some embodiments, a plurality of second discharge pipes and a plurality of second baffles are provided in the pre-cooling section, and the plurality of second baffles are arranged at intervals in the pre-cooling section to form a second serpentine channel for the circulation of the second heat exchange medium. The second discharge pipe passes through at least a portion of the second baffle along the arrangement direction of the second baffle, and the pre-cooled adsorbent in the pre-cooling section enters the low-temperature cooling section through the second discharge pipe; by arranging a plurality of second baffles in the pre-cooling section to form a second serpentine channel, the path of the second heat exchange medium in the pre-cooling section can be increased to increase the residence time of the second heat exchange medium in the pre-cooling section, thereby allowing the second heat exchange medium and the adsorbent to fully exchange heat to cool the adsorbent, which is beneficial to improving the cooling efficiency of the adsorbent. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] FIG1 is a schematic structural diagram of a highly integrated flue gas low-temperature adsorption regeneration system according to an embodiment of the present application.

[0029] FIG2 is a schematic structural diagram of an adsorbent circulation treatment tower according to an embodiment of the present application.

[0030] FIG3 is a schematic structural diagram of an adsorbent according to an embodiment of the present application.

[0031] Figure numerals: Adsorbent circulation treatment tower 100; adsorption tower 200; inner cavity 101; regeneration section 102; pre-cooling section 103; low-temperature cooling section 104; preheating section 105; buffer section 106; first inlet 107; first outlet 108; second inlet 109; second outlet 110; third inlet 111; third outlet 112; fourth inlet 113; fourth outlet 114; first discharge pipe 2; first baffle 3; second discharge pipe 4; second baffle 5; feeding circuit 6; discharge circuit 7; breathable outer shell 8. DETAILED DESCRIPTION

[0032] The embodiments of the present application are described in detail below, and examples of the embodiments are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to be used to explain the present application, but should not be understood as limiting the present application.

[0033] The highly integrated flue gas low-temperature adsorption regeneration system according to an embodiment of the present application will be described in detail below with reference to the accompanying drawings.

[0034] As shown in Figures 1 to 3, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application includes an adsorbent circulation treatment tower 100 and an adsorption tower 200. The inner cavity 101 of the adsorbent circulation treatment tower 100 is divided into a regeneration section 102, a pre-cooling section 103 and a low-temperature cooling section 104 arranged in sequence along the up and down directions. The regeneration section 102 is used to heat the adsorbent to be regenerated to a first temperature so that the adsorbent to be regenerated is desorbed and regenerated, and the pre-cooling section 103 is used to pre-cool the regenerated adsorbent from the regeneration section 102 to a second temperature. The low-temperature cooling section 104 is used to further cool the pre-cooled adsorbent from the pre-cooling section 103 to a third temperature, wherein the first temperature is higher than the second temperature, the second temperature is higher than the third temperature, and the third temperature is below room temperature.

[0035] The adsorbent circulation treatment tower 100 has a feed port and a discharge port. The feed port is used to supply the adsorbent to be regenerated into the regeneration section 102 , and the discharge port is used to discharge the low-temperature adsorbent from the low-temperature cooling section 104 .

[0036] The adsorption tower 200 has a feed port and a discharge port. A feed loop 6 is provided between the feed port of the adsorption tower 200 and the discharge port of the adsorbent circulation treatment tower 100 for transporting the low-temperature adsorbent discharged from the adsorbent circulation treatment tower 100 into the adsorption tower 200 to perform low-temperature adsorption purification on the flue gas in the adsorption tower 200. A discharge loop 7 is provided between the discharge port of the adsorption tower 200 and the feed port of the adsorbent circulation treatment tower 100 for transporting the adsorbent to be regenerated discharged from the adsorption tower 200 into the adsorbent circulation treatment tower 100 to heat the adsorbent to be regenerated in the adsorbent circulation treatment tower 100 for desorption and regeneration, and to cool the regenerated adsorbent into a low-temperature adsorbent.

[0037] In the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application, during operation, the adsorbent to be regenerated in the adsorption tower 200 is sent into the adsorbent circulation treatment tower 100 through the discharge loop 7. The adsorbent entering the adsorbent circulation treatment tower 100 passes through the regeneration section 102, the pre-cooling section 103 and the low-temperature cooling section 104 in sequence. After the regenerated adsorbent is heated to the first temperature in the regeneration section 102, the desorbed rich gas containing nitrogen oxides and sulfides is discharged from the adsorbent circulation treatment tower 100.

[0038] Since the temperature of the adsorbent after desorption and regeneration is relatively high (for example, about 300°C), the regenerated adsorbent flowing through the pre-cooling section 103 can exchange heat with the cooling medium in the pre-cooling section 103 and be pre-cooled to a second temperature (for example, about 80°C) to remove part of the heat carried by the regenerated adsorbent, thereby achieving pre-cooling of the regenerated adsorbent.

[0039] After the pre-cooled adsorbent enters the low-temperature cooling section 104, most of the heat carried by the regenerated adsorbent has been pre-cooled and removed by the cooling medium in the pre-cooling section 103. At this time, the total amount of heat carried by the pre-cooled adsorbent has been greatly reduced. Therefore, the pre-cooled adsorbent exchanges heat with the low-temperature cooling medium introduced in the low-temperature cooling section 104 and is quickly cooled to a third temperature (e.g., below room temperature, preferably below zero, e.g., -80°C to -5°C) to form a low-temperature adsorbent. The low-temperature adsorbent cooled to below room temperature in the adsorbent circulation treatment tower 100 can be directly fed into the adsorption tower 200 through the feeding loop 6 to perform low-temperature adsorption on the flue gas entering the adsorption tower 200.

[0040] Therefore, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application can not only desorb and regenerate the adsorbent to be regenerated, but also pre-cool and low-temperature cool the adsorbent in the circulation treatment tower 100 to below room temperature through the regeneration section 102, pre-cooling section 103 and low-temperature cooling section 104 arranged in sequence along the up and down directions in the adsorbent circulation treatment tower 100, so that the adsorbent circulation treatment tower 100 integrates multiple functions of regeneration, pre-cooling and low-temperature cooling, thereby making the flue gas low-temperature adsorption regeneration system highly integrated.

[0041] Moreover, the adsorbent to be regenerated in the adsorption tower 200 is input into the adsorbent circulation treatment tower 100 through the discharge loop 7 for desorption and cooling to below room temperature. The low-temperature adsorbent after desorption and regeneration can be directly returned to the adsorption tower 200 through the feeding loop 6 for low-temperature adsorption of the flue gas, thereby realizing low-temperature adsorption and desorption regeneration of the adsorbent between the adsorption tower 200 and the adsorbent circulation treatment tower 100. In other words, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application can no longer be separately provided with a spray cooling tower for cooling the flue gas and sending the low-temperature flue gas into the adsorption tower for low-temperature adsorption, as well as the connecting pipelines between the spray cooling tower and the adsorption tower 200 and the adsorbent circulation treatment tower 100, thereby reducing the number of system equipment and connecting pipelines, making the system simple, simplifying the process, reducing the floor space, improving the integration of the system, reducing costs, and improving the flue gas treatment efficiency.

[0042] Therefore, the highly integrated flue gas low-temperature adsorption regeneration system of the embodiment of the present application has the advantages of simple system, simplified process, small occupied area, high integration, high flue gas treatment efficiency and low cost.

[0043] As shown in FIG3 , in an embodiment of the present application, an adsorbent can be filled in a breathable housing 8 to form an adsorption unit. The adsorbent can be a granular or powdered adsorbent, or can be an adsorbent body made of a powdered or granular adsorbent. For example, the powdered or granular adsorbent can be formed into a spherical body or a cylindrical body by a binder. Of course, the adsorbent body can be further provided with a protective layer, such as a breathable membrane covering the outside of the adsorbent body, to further enhance the strength of the adsorbent body.

[0044] The breathable housing 8 has air holes through which smoke can enter the housing 8. The smoke can then pass through the gaps between adjacent adsorbents and / or the pores within the adsorbents themselves, thereby reducing direct collisions, friction, and wear between adsorbents, as well as dust generation. The breathable housing 8 can be in the shape of a spherical, cylindrical, or other rotating body. The diameter of the breathable housing 8 can range from 10 mm to 100 mm, and the diameter of the adsorbent can range from 1 mm to 10 mm.

[0045] By placing the adsorbent in the breathable shell 8 to form an adsorption unit, on the one hand, the dust generated by the collision between the adsorbents can be reduced; on the other hand, it is beneficial to increase the contact area between the flue gas and the adsorbent and improve the air permeability of the adsorbent, which is particularly beneficial for low-temperature adsorption.

[0046] In some embodiments, the heights of the regeneration section 102, the pre-cooling section 103 and the low-temperature cooling section 104 are all the same. Since the adsorbent moves under the action of its own gravity, the adsorbent can stay in each section of the regeneration section 102, the pre-cooling section 103 and the low-temperature cooling section 104 in the adsorbent circulation treatment tower 1 for the same time, so as to avoid the adsorbent being unable to be fully heated and cooled due to the length of a certain section being too long or too short.

[0047] In some embodiments, in the regeneration section 102 , the adsorbent to be regenerated is indirectly heat-exchanged with the first heat exchange medium to heat the adsorbent to be regenerated.

[0048] It can be understood that since the adsorbent to be regenerated needs to be desorbed in the regeneration section 102, direct contact between the adsorbent and the first heat exchange medium can be avoided by indirectly exchanging heat between the adsorbent and the first heat exchange medium, thereby avoiding the first heat exchange medium from adhering to the surface of the adsorbent, thereby reducing the separation rate between the gas desorbed from the adsorbent and the adsorbent, which is beneficial to improving the desorption efficiency of the adsorbent.

[0049] In some embodiments, in the pre-cooling section 103 , the regenerated adsorbent is indirectly heat-exchanged with the second heat exchange medium to pre-cool the regenerated adsorbent.

[0050] When the regenerated adsorbent just enters the pre-cooling section 103 from the regeneration section 102, the temperature of the regenerated adsorbent still has the relatively high first temperature. By indirectly exchanging heat between the regenerated adsorbent and the second heat exchange medium in the pre-cooling section 103, the second heat exchange medium can be prevented from adhering to the surface of the regenerated adsorbent, thereby reducing the separation rate of the gas desorbed from the regenerated adsorbent and the adsorbent.

[0051] In some embodiments, the first temperature is not less than 300°C.

[0052] For example, the first temperature is 350°C, 380°C, or 400°C. It is understood that the desorption rate of the adsorbent to be regenerated is positively correlated with the heating temperature. In other words, the higher the heating temperature of the adsorbent, the higher the desorption efficiency of the adsorbent. However, the temperature required to heat the adsorbent is correspondingly higher, which in turn increases the cost. Therefore, the first temperature can be reasonably set based on the desorption efficiency requirements of different adsorbents, thereby balancing the desorption efficiency and cost of the adsorbent.

[0053] In some embodiments, the second temperature is 30°C to 150°C.

[0054] For example, the second temperature is 30°C, 80°C, 120°C or 150°C. If the second temperature is set too high, the difference between the second temperature and the first temperature is small, and the difference between the second temperature and the third temperature is large, which will weaken the effect of cooling the adsorbent step; if the second temperature is set too low, the difference between the second temperature and the first temperature is large, and the difference between the second temperature and the third temperature is small, which will also weaken the effect of cooling the adsorbent step. Therefore, the adsorbent circulation treatment tower 100 of the embodiment of the present application sets the second temperature between 30°C and 150°C, so that the temperature difference between the second temperature and the first temperature, and between the second temperature and the third temperature will not be too large or too small, thereby weakening the effect of cooling the adsorbent step, which is further conducive to saving energy consumption.

[0055] In some embodiments, the third temperature is -80°C to -5°C.

[0056] For example, the third temperature is -80°C, -30°C, or -5°C. It is understandable that the adsorption efficiency of the adsorbent is positively correlated with its temperature, that is, the lower the temperature of the adsorbent, the higher the adsorption efficiency of the adsorbent. However, if the temperature of the adsorbent is set too low, the temperature of the corresponding heat exchange medium will be set too low, resulting in higher costs for producing heat exchange media with lower temperatures. Therefore, the third temperature can be reasonably set according to the adsorption efficiency requirements of different adsorbents, taking into account both the adsorption efficiency and cost of the adsorbent.

[0057] In some embodiments, in the low-temperature cooling section 104 , the pre-cooled adsorbent is subjected to direct contact heat exchange with the third heat exchange medium to further cool the adsorbent.

[0058] After the regenerated adsorbent is pre-cooled in the pre-cooling section 103, the temperature of the pre-cooled adsorbent drops to a second temperature. Since the second temperature is lower than the first temperature, desorption of the pre-cooled adsorbent in the low-temperature cooling section 104 does not occur. In other words, contact between the adsorbent and the third heat exchange medium in the low-temperature cooling section 104 does not affect the adsorbent. In addition, by directly exchanging heat between the adsorbent and the third heat exchange medium, the heat carried by the pre-cooled adsorbent can be quickly transferred to the third heat exchange medium, and the third heat exchange medium carries the heat out of the low-temperature cooling section 104, thereby quickly cooling the pre-cooled adsorbent and improving the cooling efficiency of the adsorbent in the low-temperature cooling section 104.

[0059] In some embodiments, the first heat exchange medium is high-temperature air having a temperature higher than a first temperature, the second heat exchange medium is room-temperature air, and the third heat exchange medium is low-temperature air having a temperature not higher than a third temperature.

[0060] In the embodiment of the present application, the second heat exchange medium is set to room temperature air, which makes the second heat exchange medium easy to obtain and low in cost. The third heat exchange medium is low-temperature air, which can be obtained by simply cooling room temperature air using a cooling device, making the third heat exchange medium easy to process and manufacture and low in cost.

[0061] In some embodiments, a first pipeline is provided between the pre-cooling section 103 and the low-temperature cooling section 104 for transporting the third heat exchange medium discharged from the low-temperature cooling section 104 after heat exchange into the pre-cooling section 103 .

[0062] For example, as shown in Figure 2, the low-temperature cooling section 104 on the adsorbent circulation treatment tower 1 has a first inlet 107 and a first outlet 108, the pre-cooling section 103 on the adsorbent circulation treatment tower 1 has a second inlet 109 and a second outlet 110, and a first pipeline is provided between the first outlet 108 and the second inlet 109.

[0063] In some embodiments, the third heat exchange medium enters the low-temperature cooling section 104 of the adsorbent circulation treatment tower 1 through the first inlet 107, exchanges heat with the adsorbent in the low-temperature cooling section 104, and is discharged into the first pipeline through the first outlet 108. The temperature of the third heat exchange medium discharged into the first pipeline is reduced after heat exchange with the adsorbent. The third heat exchange medium with reduced temperature forms a second heat exchange medium and enters the pre-cooling section 103 through the second inlet 109 to cool the adsorbent in the pre-cooling section 103.

[0064] Therefore, only a third heat exchange medium needs to be provided to achieve step-by-step cooling of the adsorbent, which makes full use of the heat exchange medium and avoids the need to set up a second heat exchange medium separately to cool the adsorbent in the pre-cooling section 103, thereby greatly reducing the manufacturing cost of the heat exchange medium. This not only improves the utilization rate of the heat exchange medium but also saves costs.

[0065] In an embodiment of the present application, the adsorbent circulation treatment tower 100 may include a heater (not shown), and a second pipeline is provided between the heater and the pre-cooling section 103 for transporting the second heat exchange medium after heat exchange in the pre-cooling section 103 to the heater. A third pipeline is provided between the heater and the regeneration section 102, and the heater heats the second heat exchange medium after heat exchange and transports it as the first heat exchange medium to the regeneration section 102 through the third pipeline.

[0066] For example, as shown in Figure 2, a third inlet 111 and a third outlet 112 are provided at a position corresponding to the regeneration section 102 on the adsorbent circulation treatment tower 1, the second outlet 110 is connected to the heater through a second pipeline, and the heater is connected to the third inlet 111 through a third pipeline.

[0067] In some embodiments, the second heat exchange medium enters the heater through the second pipeline, is heated by the heater to form the first heat exchange medium, and enters the regeneration section 102 through the third pipeline. After exchanging heat with the adsorbent in the regeneration section 102, it is discharged from the regeneration section 102 through the third outlet 112, thereby achieving heating of the adsorbent.

[0068] Therefore, by setting up a heater, the second heat exchange medium is heated and then input into the regeneration section 102 as the first heat exchange medium, thereby achieving full utilization of the heat exchange medium. It can avoid setting up a first heat exchange medium separately to cool the adsorbent in the pre-cooling section 103, greatly reducing the manufacturing cost of the heat exchange medium, not only improving the utilization rate of the heat exchange medium, but also saving costs.

[0069] In some embodiments, the inner cavity 101 of the adsorbent circulation treatment tower 1 further has a preheating section 105 located above the regeneration section 102. The first heat exchange medium discharged from the regeneration section 102 after heat exchange enters the preheating section 105 through a fourth pipeline to preheat the adsorbent.

[0070] For example, as shown in FIG2 , a fourth inlet 113 and a fourth outlet 114 are provided on the adsorbent circulation treatment tower 1 at a position corresponding to the regeneration section 102 , and the third outlet 112 is connected to the preheating section 105 through a fourth pipeline.

[0071] In some embodiments, the first heat exchange medium enters the preheating section 105 through the fourth pipeline, preheating the adsorbent in the preheating section 105, thereby recovering and utilizing the residual heat after the first heat exchange medium is heated, thereby preventing waste of the residual heat after the first heat exchange medium is heated. In addition, the adsorbent circulation treatment tower 100 of the present embodiment preheats the adsorbent so that the adsorbent can be rapidly heated and desorbed in the regeneration section 102, thereby facilitating rapid desorption and regeneration of the adsorbent in the regeneration section 102, thereby facilitating improved regeneration efficiency of the adsorbent circulation treatment tower 100 of the present embodiment.

[0072] In some embodiments, the height of the preheating section 105 is less than the height of the regeneration section 102. Since the preheating section 105 is used to preliminarily heat the adsorbent, its height can be set smaller to reduce the overall height of the adsorbent circulation treatment tower 1 and avoid manufacturing difficulties due to its excessive height.

[0073] In some embodiments, the inner cavity 101 of the adsorbent circulation treatment tower 1 further has a buffer section 106 , which is disposed between the regeneration section 102 and the pre-cooling section 103 .

[0074] As shown in Figure 2, a buffer section 106 is set between the regeneration section 102 and the pre-cooling section 103. The adsorbent flowing out of the regeneration section 102 can be buffered in the buffer section 106, for example, remixed, so that the desorbed rich gas can be better separated from the adsorbent, and the adsorbent can flow downward to the low-temperature cooling section 104 more evenly and smoothly.

[0075] In addition, due to the temperature difference between the regeneration section 102 and the pre-cooling section 103, the regeneration section 102 requires a first heat exchange medium with a higher temperature for adsorbent desorption and regeneration, and the pre-cooling section 103 requires a second heat exchange medium with a lower temperature for adsorbent cooling. The adsorbent in the buffer section 106 can isolate the regeneration section 102 and the low-temperature cooling section 104, preventing the temperatures between the regeneration section 102 and the pre-cooling section 103 from affecting each other, which is beneficial to improving the working reliability of the regeneration section 102 and the pre-cooling section 103.

[0076] In some embodiments, the height of the buffer section 106 is smaller than that of the regeneration section 102 and the pre-cooling section 103. Since the buffer section 106 is used to buffer the adsorbent, its height can be set smaller to reduce the overall height of the adsorbent circulation treatment tower 1 and avoid manufacturing difficulties due to its excessive height.

[0077] In some embodiments, a plurality of first discharge pipes 2 and a plurality of first baffles 3 are provided in the regeneration section 102. The plurality of first baffles 3 are arranged at intervals in the regeneration section 102 to form a first serpentine channel for the circulation of the first heat exchange medium. The first discharge pipe 2 passes through at least a portion of the first baffle 3 along the arrangement direction of the first baffle 3, and the adsorbent in the regeneration section 102 enters the pre-cooling section 103 through the first discharge pipe 2.

[0078] For example, as shown in Figure 2, the third inlet 111 is connected to one port of the first serpentine channel, and the third outlet 112 is in communication with the other port of the first serpentine channel. By arranging multiple first baffles 3 in the regeneration section 102 to form a first serpentine channel, the path of the first heat exchange medium in the regeneration section 102 can be increased, so as to increase the residence time of the first heat exchange medium in the regeneration section 102, thereby allowing the first heat exchange medium and the adsorbent to be regenerated to fully exchange heat, so that the adsorbent can be quickly decomposed, which is beneficial to improving the desorption and regeneration efficiency of the adsorbent.

[0079] In some embodiments, the thickness of the first baffle 3 is 5 mm to 10 mm. In some embodiments, the thickness of the first baffle 3 is 8 mm. If the thickness of the first baffle 3 is set too small, the strength of the first baffle 3 is poor, resulting in poor working reliability. If the first baffle 3 is set too thick, material costs will be wasted.

[0080] In some embodiments, a plurality of second discharge pipes 4 and a plurality of second baffles 5 are provided in the pre-cooling section 103. The plurality of second baffles 5 are arranged at intervals in the pre-cooling section 103 to form a second serpentine channel for the circulation of the second heat exchange medium. The second discharge pipe 4 passes through at least a portion of the second baffle 5 in the up and down directions, and the adsorbent in the pre-cooling section 103 enters the low-temperature cooling section 104 through the second discharge pipe 4.

[0081] For example, as shown in Figure 2, the second inlet 109 is connected to one port of the second serpentine channel, and the second outlet 110 is in communication with the other port of the second serpentine channel. By arranging a plurality of second deflectors 5 in the pre-cooling section 103 to form a second serpentine channel, the path of the second heat exchange medium in the pre-cooling section 103 can be increased to increase the residence time of the second heat exchange medium in the pre-cooling section 103, thereby allowing the second heat exchange medium and the regenerated adsorbent to fully exchange heat, so as to pre-cool the adsorbent, which is beneficial to improving the cooling efficiency of the adsorbent.

[0082] In the description of the present application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present application.

[0083] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of the technical features being referred to. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of such features. Throughout the description of this application, "plurality" means at least two, for example, two, three, etc., unless otherwise specifically defined.

[0084] In this application, unless otherwise specified or limited, the terms "installed," "connected," "connect," "fixed," etc. should be understood in a broad sense. For example, they can refer to fixed connection, detachable connection, or integration; mechanical connection, electrical connection, or communication; direct connection or indirect connection through an intermediate medium; internal communication between two elements or interaction between two elements, unless otherwise specified. Those skilled in the art will understand the specific meanings of the above terms in this application based on specific circumstances.

[0085] In this application, unless otherwise expressly specified or limited, when a first feature is "above" or "below" a second feature, it may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Furthermore, when a first feature is "above," "above," or "above" a second feature, it may mean that the first feature is directly above or diagonally above the second feature, or simply means that the first feature is at a higher level than the second feature. When a first feature is "below," "below," or "below" a second feature, it may mean that the first feature is directly below or diagonally below the second feature, or simply means that the first feature is at a lower level than the second feature.

[0086] In this application, the terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art can combine and combine different embodiments or examples described in this specification and the features of different embodiments or examples without contradiction.

[0087] Although the above embodiments have been shown and described, it is understood that the above embodiments are illustrative and cannot be understood as limitations on the present application. Changes, modifications, substitutions and variations of the above embodiments made by ordinary technicians in this field are all within the scope of protection of the present application.

Claims

1. A highly integrated flue gas low-temperature adsorption regeneration system, comprising: An adsorbent circulation treatment tower, wherein the inner cavity of the adsorbent circulation treatment tower is divided into a regeneration section, a pre-cooling section and a low-temperature cooling section arranged in sequence along the upper and lower directions, the regeneration section is used to heat the adsorbent to be regenerated to a first temperature so that the adsorbent to be regenerated is desorbed and regenerated, the pre-cooling section is used to pre-cool the regenerated adsorbent from the regeneration section to a second temperature, and the low-temperature cooling section is used to further cool the pre-cooled adsorbent from the pre-cooling section to a third temperature to become a low-temperature adsorbent, wherein the first temperature is higher than the second temperature, the second temperature is higher than the third temperature, and the third temperature is below room temperature, and the adsorbent circulation treatment tower has a feed port and a discharge port, the feed port is used to supply the adsorbent to be regenerated into the regeneration section, and the discharge port is used to discharge the low-temperature adsorbent from the low-temperature cooling section; and An adsorption tower having a feeding port and a discharging port, a feeding circuit is provided between the feeding port of the adsorption tower and the discharging port of the adsorbent circulation treatment tower, for conveying the low-temperature adsorbent discharged from the adsorbent circulation treatment tower into the adsorption tower so as to perform low-temperature adsorption purification on the flue gas in the adsorption tower, a discharging circuit is provided between the discharging port of the adsorption tower and the feeding port of the adsorbent circulation treatment tower, for conveying the adsorbent to be regenerated discharged from the adsorption tower into the adsorbent circulation treatment tower, for heating the adsorbent to be regenerated in the adsorbent circulation treatment tower so as to desorb and regenerate it and cool the regenerated adsorbent into the low-temperature adsorbent.

2. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 1, wherein: In the regeneration section, the adsorbent to be regenerated is subjected to indirect heat exchange with a first heat exchange medium to heat the adsorbent to be regenerated for desorption and regeneration; and / or In the pre-cooling section, the regenerated adsorbent is subjected to indirect heat exchange with a second heat exchange medium to pre-cool the regenerated adsorbent; and / or In the low-temperature cooling section, the pre-cooled adsorbent is in direct contact with a third heat exchange medium for heat exchange, so as to further cool the adsorbent to form the low-temperature adsorbent.

3. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 2, wherein: The first heat exchange medium is high-temperature air having a temperature higher than the first temperature, the second heat exchange medium is room-temperature air, and the third heat exchange medium is low-temperature air having a temperature lower than the third temperature.

4. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 3, wherein: A first pipeline is provided between the pre-cooling section and the low-temperature cooling section for conveying the third heat exchange medium discharged from the low-temperature cooling section after heat exchange into the pre-cooling section.

5. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 4 further includes a heater, a second pipeline is provided between the heater and the pre-cooling section, which is used to transport the second heat exchange medium discharged from the pre-cooling section to the heater, and a third pipeline is provided between the heater and the regeneration section, and the heater heats the second heat exchange medium after heat exchange into the first heat exchange medium and transports it to the regeneration section through the third pipeline.

6. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 2, wherein: The inner cavity of the adsorbent circulation treatment tower also has a preheating section located above the regeneration section. The first heat exchange medium after heat exchange discharged from the regeneration section enters the preheating section through a fourth pipeline to preheat the adsorbent in the preheating section.

7. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 2, wherein: The inner cavity of the adsorbent circulation treatment tower further has a buffer section for buffering the adsorbent, and the buffer section is arranged between the regeneration section and the pre-cooling section.

8. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 7, wherein: A plurality of first discharge pipes and a plurality of first baffles are provided in the regeneration section. The plurality of first baffles are arranged at intervals in the regeneration section to form a first serpentine channel for the circulation of the first heat exchange medium. The first discharge pipe passes through at least a portion of the first baffle in the up and down directions. The adsorbent desorbed and regenerated in the regeneration section enters the pre-cooling section through the first discharge pipe.

9. The highly integrated flue gas low-temperature adsorption regeneration system according to claim 8, wherein: A plurality of second feed pipes and a plurality of second baffles are provided in the pre-cooling section. The plurality of second baffles are arranged at intervals in the pre-cooling section to form a second serpentine channel for the circulation of the second heat exchange medium. The second feed pipe passes through at least a portion of the second baffle in the up and down directions. The pre-cooled adsorbent in the pre-cooling section enters the low-temperature cooling section through the second feed pipe.

10. The highly integrated flue gas low-temperature adsorption regeneration system according to any one of claims 1 to 9, wherein: The first temperature is not less than 300°C; and / or The second temperature is 30°C to 150°C; and / or The third temperature is -80°C to -5°C.

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