Regeneration device coupled with flue gas waste heat recovery and low-temperature adsorption regeneration system

Abstract

Disclosed are a regeneration device coupled with flue gas waste heat recovery and a low-temperature adsorption regeneration system. The regeneration system comprises a regeneration tower and an air preheater. A hot-side inlet of the air preheater is communicated with a flue gas outlet of an economizer, a cold-side inlet of the air preheater is communicated with a blower, and a cold-side outlet of the air preheater is communicated with a heating inlet; high-temperature air enters a heating section via the heating inlet to heat an adsorbent; a cooling outlet and a heating outlet are communicated with a preheating inlet by means of a pipe; and mixed gas enters a preheating section via the preheating inlet to preheat the adsorbent.

Description

Regeneration device coupled with flue gas waste heat recovery and low-temperature adsorption regeneration system

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] This application claims priority to Chinese patent application No. 2024100965395 filed in China on January 23, 2024, the entire contents of which are incorporated herein by reference. Technical Field

[0003] The present disclosure relates to the technical field of flue gas purification, and in particular to a regeneration device coupled with flue gas waste heat recovery and a low-temperature adsorption regeneration system. Background Art

[0004] Coal-fired flue gas produces a large amount of pollutants, which is one of the important factors that endanger the atmospheric environment and human health. In the related art, the flue gas discharged from the boiler (about 200°C) is passed into an adsorption tower filled with adsorbent for high-temperature adsorption purification, and the adsorbent saturated with adsorption enters the regeneration tower for heating and regeneration. However, high-temperature flue gas adsorption has the problem of poor adsorption effect, high nitrogen oxide content in the clean flue gas after adsorption, and inability to achieve near-zero emissions. In order to overcome the problem of high-temperature adsorption, a flue gas low-temperature adsorption technology is proposed in the related art, that is, the flue gas is cooled to low-temperature flue gas below room temperature, for example, and then the pollutants in the flue gas are adsorbed and removed by adsorbent. In low-temperature adsorption, the adsorption capacity of the adsorbent is increased exponentially under low-temperature conditions, which greatly improves the adsorption purification rate compared with conventional high-temperature flue gas adsorption, and can achieve near-zero emissions of flue gas.

[0005] However, through research, the inventors realized that the saturated adsorbent discharged from the high-temperature adsorption tower has a relatively high temperature (above 180°C). The heating load required to heat this high-temperature adsorbent to the regeneration tower (250°C-350°C) is relatively low, and the traditional one-stage heating method can meet the heating requirements. During the low-temperature adsorption process, however, the adsorbent's discharge temperature is relatively low (e.g., below room temperature) due to contact with the low-temperature flue gas. Using a conventional one-stage heating regeneration tower to heat and regenerate the adsorbent places a high load on the heater, resulting in high regeneration energy consumption and costs, hindering the further development of low-temperature flue gas adsorption technology. Summary of the Invention

[0006] The present disclosure aims to solve at least one of the technical problems in the related art to a certain extent. To this end, a first embodiment of the present disclosure proposes a regeneration device coupled with flue gas waste heat recovery.

[0007] A second embodiment of the present disclosure provides a low-temperature adsorption regeneration system.

[0008] The regeneration device coupled with flue gas waste heat recovery according to the first embodiment of the present disclosure comprises: a regeneration tower, which is divided from top to bottom into a preheating section for preheating an adsorbent, a heating section for heating the preheated adsorbent to regenerate and desorb the adsorbent, and a cooling section for cooling the regenerated adsorbent, the preheating section being provided with a preheating inlet and a preheating outlet, the heating section being provided with a heating inlet and a heating outlet, the cooling section being provided with a cooling inlet and a cooling outlet, the cooling inlet being used to supply cooling gas to enter the cooling section to cool the adsorbent; an air preheater, the hot side inlet of the air preheater being connected to the flue gas outlet of the economizer, The cold side inlet of the air preheater is connected to the blower, and the cold side outlet of the air preheater is connected to the heating inlet. The flue gas input into the air preheater from the economizer exchanges heat with the gas input into the air preheater from the blower to heat the gas input into the air preheater from the blower into high-temperature air, and then input into the heating section through the heating inlet. The cooling outlet is connected to the heating outlet and the preheating inlet, so that the cooling gas discharged from the cooling section and the air discharged from the heating outlet are mixed into a mixed gas and then enter the preheating section to preheat the adsorbent in the preheating section.

[0009] The regeneration device coupled with flue gas waste heat recovery provided by the embodiment of the present disclosure realizes multi-stage heating regeneration by arranging a preheating section, a heating section and a cooling section in the regeneration tower, that is, the adsorbent is first preheated in the preheating section, and then the preheated adsorbent is heated, which reduces the temperature rise range of the adsorbent in the heating section, effectively alleviates the heating load of the heating device, reduces the energy consumption of the regeneration device, reduces the operating cost of the regeneration device, and is also beneficial to increase the residence time of the adsorbent in the regeneration tower, so that the regeneration of the adsorbent is more thorough.

[0010] The disclosed embodiment utilizes the waste heat in the high-temperature flue gas flowing out of the economizer to heat and regenerate the adsorbent in the heating section. The air with waste heat discharged from the heating section and the cooling gas with a certain amount of heat discharged from the cooling section are mixed and then input into the preheating section for utilization to preheat the adsorbent, thereby achieving efficient utilization of the waste heat of the flue gas, realizing the cascade recovery and utilization of energy, reducing the energy consumption of the regeneration system, and reducing the operating costs of the regeneration system. In addition, the provision of the cooling section allows the adsorbent to be cooled to a certain extent before leaving the tower. The cooled adsorbent is transported to the adsorption tower for adsorption, which reduces the contact temperature between the adsorbent and the flue gas in the adsorption tower, helping to improve the adsorption efficiency of the adsorption tower.

[0011] In some embodiments, the ratio of cooling gas supplied from the cooling outlet to the preheating inlet to air supplied from the heating outlet to the preheating inlet is adjustable to adjust the temperature of the mixed gas. The ratio of the heat-exchanged cooling gas flowing out of the cooling outlet and the heat-exchanged high-temperature air flowing out of the heating outlet within the pipeline is adjustable, thereby adjusting the temperature of the mixed gas, thereby adjusting the preheating temperature of the preheating section, preventing insufficient preheating temperature in the preheating section, and preventing water vapor released during the adsorbent preheating process in the preheating section from condensing and agglomerating on the adsorbent, thereby causing blockage of the feed pipe.

[0012] In some embodiments, the preheating section has a first flow channel for circulating the mixed gas, the heating section has a second flow channel for circulating the high-temperature air, and the cooling section has a third flow channel for circulating the cooling gas. At least one of the first flow channel, the second flow channel, and the third flow channel is a serpentine flow channel to extend the residence time of the gas in the regeneration tower, thereby achieving a better heat exchange effect and improving energy utilization efficiency.

[0013] In some embodiments, a plurality of horizontally arranged baffles are provided in the regeneration tower, and the baffles are spaced apart in the vertical direction to define the serpentine first flow channel, the serpentine second flow channel, and the serpentine third flow channel.

[0014] In some embodiments, the preheating section is provided with a plurality of first discharge pipes, the heating section is provided with a plurality of second discharge pipes, and the cooling section is provided with a plurality of third discharge pipes. The first discharge pipes, the second discharge pipes, and the third discharge pipes all extend vertically and are used to drop the adsorbent. The adsorbent entering from the regeneration inlet flows sequentially through the first discharge pipes, the second discharge pipes, and the third discharge pipes before being discharged from the regeneration outlet.

[0015] In some embodiments, a distribution cavity for forming a distribution layer is provided above the first discharge pipe. A first transition cavity for forming a first material layer is provided between the preheating section and the heating section. A second transition cavity for forming a second material layer is provided between the heating section and the cooling section. The distribution cavity is provided with a first suction port located above the material layer. The first suction port is used to promptly extract regeneration gas generated in the preheating section and the material layer to prevent blockage caused by material agglomeration.

[0016] In some embodiments, the first transition chamber is provided with a second suction port, and / or the second transition chamber is provided with a third suction port. The second suction port and the third suction port are used to promptly extract the regeneration gas to avoid blockage caused by material agglomeration.

[0017] In some embodiments, in the preheating section, the mixed gas preheats the adsorbent to 50°C-110°C; in the heating section, the high-temperature air heats the adsorbent to 150°C-350°C; and in the cooling section, the cooling gas cools the adsorbent to 50°C-100°C. In some embodiments, in the preheating section, the mixed gas initially heats the adsorbent to 100°C; in the heating section, the high-temperature air heats the adsorbent to 300°C to desorb and regenerate the adsorbent; and in the cooling section, the cooling gas cools the adsorbent to 80°C.

[0018] A low-temperature adsorption regeneration system according to an embodiment of the second aspect of the present disclosure includes: an adsorption tower, the adsorption tower having a flue gas inlet and a flue gas outlet, low-temperature flue gas below room temperature enters the adsorption tower from the flue gas inlet and contacts with an adsorbent to be adsorbed and purified by the adsorbent into clean flue gas and discharged from the flue gas outlet; a regeneration device, the regeneration device being a regeneration device coupled with flue gas waste heat recovery in any embodiment of the first aspect above, the adsorption saturated adsorbent discharged from the adsorption tower being regenerated in the regeneration device and the regenerated adsorbent being transported back to the adsorption tower.

[0019] In some embodiments, the flue gas outlet is connected to the cooling inlet, and the clean flue gas output from the flue gas outlet is input into the cooling section as the cooling gas to indirectly cool the adsorbent in the cooling section, thereby fully utilizing the cold energy in the low-temperature flue gas. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] FIG1 is a schematic structural diagram of a regeneration device coupled with flue gas waste heat recovery according to an embodiment of the present disclosure.

[0021] FIG2 is a schematic diagram of the interior of a regeneration tower provided in an embodiment of the present disclosure.

[0022] Figure numerals: Regeneration system 100, regeneration tower 110, preheating section 111, preheating inlet 1111, preheating outlet 1112, first flow channel 1113, heating section 112, heating inlet 1121, heating outlet 1122, second flow channel 1123, cooling section 113, cooling inlet 1131, cooling outlet 1132, third flow channel 1133, regeneration inlet 115, regeneration outlet 116, first discharge pipe 1171, second discharge pipe 1172, third discharge pipe 1173, cloth layer 1181, first pile layer 1182, second pile layer 1183, first suction port 1191, second suction port 1192, third suction port 1193, air preheater 120, hot side inlet 121, cold side inlet 122, cold side outlet 123, blower 130, baffle 140. DETAILED DESCRIPTION

[0023] The embodiments of the present disclosure 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 disclosure, but should not be understood as limiting the present disclosure.

[0024] The following describes a regeneration device coupled with flue gas waste heat recovery according to an embodiment of the first aspect of the present disclosure with reference to Figures 1 and 2. The regeneration system 100 includes a regeneration tower 110 and an air preheater 120.

[0025] The regeneration tower 110 is divided from top to bottom into a preheating section 111, a heating section 112, and a cooling section 113. The adsorbent passes through these three sections from top to bottom. The preheating section 111 is used to preheat the adsorbent, while the heating section 112 is used to heat the preheated adsorbent for regeneration and desorption. The cooling section 113 is used to cool the regenerated adsorbent.

[0026] The preheating section 111 is provided with a preheating inlet 1111 and a preheating outlet 1112. The heating section 112 is provided with a heating inlet 1121 and a heating outlet 1122. The cooling section 113 is provided with a cooling inlet 1131 and a cooling outlet 1132. The cooling inlet 1131 is used to allow cooling gas to enter the cooling section 113 to cool the adsorbent. In other words, the cooling gas enters the cooling section 113 from the cooling inlet 1131 to cool the adsorbent. In some embodiments, the cooling gas is cooling air.

[0027] The air preheater 120 has a hot side and a cold side. The hot side inlet 121 of the air preheater 120 is connected to the flue gas outlet of the economizer, and the high-temperature flue gas from the economizer enters the hot side inlet 121. The cold side inlet 122 of the air preheater 120 is connected to the blower 130. The cold side outlet 123 of the air preheater 120 is connected to the heating inlet 1121 of the regeneration tower 110. In the air preheater 120, the flue gas from the economizer enters the air preheater 120 through heat exchange with the gas from the blower 130, heating the gas from the blower 130 to high-temperature air. The high-temperature air then enters the heating section 112 through the heating inlet 1121, heating the adsorbent to complete desorption.

[0028] The cooling outlet 1132 is connected to the heating outlet 1122 and the preheating inlet 1111, so that the cooling gas discharged from the cooling section 113 and the air discharged from the heating outlet 1122 mix to form a mixed gas, which then enters the preheating section 111 to preheat the adsorbent within the preheating section 111. The gas flowing out of the cooling outlet 1132 of the cooling section 113 carries a certain amount of heat, while the air flowing out of the heating outlet 1122 of the heating section 112 still has a large amount of residual heat. The two gases mix, and the mixed gas enters the preheating section 111 through the preheating inlet 1111 to preheat the adsorbent, fully utilizing the heat of both gases.

[0029] The adsorbent circulates from top to bottom, undergoing preheating, heating regeneration, and cooling in sequence. Specifically, the mixed gas initially heats the adsorbent entering the regeneration tower 110 in the preheating section 111, i.e., preheating it. High-temperature air further heats the preheated adsorbent in the heating section 112 to completely desorb the pollutants adsorbed by the adsorbent. Cooling gas cools the regenerated adsorbent after desorption in the cooling section 113. It will be appreciated that the temperature of the high-temperature air is higher than that of the mixed gas.

[0030] The regeneration device coupled with flue gas waste heat recovery provided by the embodiment of the present disclosure realizes multi-stage heating regeneration by arranging a preheating section, a heating section and a cooling section in the regeneration tower, that is, the adsorbent is first preheated in the preheating section, and then the preheated adsorbent is heated, which reduces the temperature rise range of the adsorbent in the heating section, effectively alleviates the heating load of the heating device, reduces the energy consumption of the regeneration device, reduces the operating cost of the regeneration device, and is also beneficial to increase the residence time of the adsorbent in the regeneration tower, so that the regeneration of the adsorbent is more thorough.

[0031] The disclosed embodiment utilizes the waste heat in the high-temperature flue gas flowing out of the economizer to heat and regenerate the adsorbent in the heating section. The air with waste heat discharged from the heating section and the cooling gas with a certain amount of heat discharged from the cooling section are mixed and then input into the preheating section for utilization to preheat the adsorbent, thereby achieving efficient utilization of the waste heat of the flue gas, realizing the cascade recovery and utilization of energy, reducing the energy consumption of the regeneration system, and reducing the operating costs of the regeneration system. In addition, the provision of the cooling section allows the adsorbent to be cooled to a certain extent before leaving the tower. The cooled adsorbent is transported to the adsorption tower for adsorption, which reduces the contact temperature between the adsorbent and the flue gas in the adsorption tower, helping to improve the adsorption efficiency of the adsorption tower.

[0032] In some embodiments, the ratio of the cooling gas supplied from the cooling outlet 1132 to the preheating inlet 1111 to the air supplied from the heating outlet 1122 to the preheating inlet 1111 is adjustable, thereby adjusting the temperature of the mixed gas entering the preheating section 111. In other words, the mixing ratio of the heat-exchanged cooling gas flowing out of the cooling outlet 1132 and the heat-exchanged high-temperature air flowing out of the heating outlet 1112 within the pipeline is adjustable, thereby adjusting the temperature of the mixed gas, and thus adjusting the preheating temperature of the preheating section 111, to prevent the preheating temperature from being too high or too low.

[0033] In some embodiments, the preheating temperature in the preheating section 111 is controlled within the range of 80 degrees Celsius to 110 degrees Celsius. If the preheating temperature in the preheating section 111 is too high (exceeding 110 degrees Celsius), a large amount of pollutants adsorbed in the adsorbent will be desorbed to generate regeneration gas, which will increase the regeneration gas extraction burden of the preheating section 111. If the preheating temperature in the preheating section 111 is too low (lower than 80 degrees Celsius), the heating pressure of the heating section 112 will be increased, and the regeneration cost will be increased. In addition, due to the insufficient preheating temperature in the preheating section 111, the water vapor released during the preheating of the adsorbent will condense and agglomerate with the adsorbent, causing blockage of the discharge pipe. Therefore, controlling the preheating temperature in the preheating section 111 within the range of 80 degrees Celsius to 110 degrees Celsius can effectively reduce the heating pressure of the heating section 112 while avoiding large-scale desorption of the adsorbent in the preheating section 111 and avoiding adsorbent agglomeration.

[0034] In some embodiments, the gas ratio can be adjusted by adjusting the flow valve or the like.

[0035] In some embodiments, as shown in FIG1 , the preheating section 111 defines a first flow channel 1113 for circulating a mixed gas, the first flow channel 1113 communicating with the preheating inlet 1111 and the preheating outlet 1112. The heating section 112 defines a second flow channel 1123 for circulating high-temperature air, the second flow channel 1123 communicating with the heating inlet 1121 and the heating outlet 1122. The cooling section 113 defines a third flow channel 1133 for circulating cooling gas. The mixed gas circulates in the first flow channel 1113 to indirectly exchange heat with the adsorbent, the high-temperature air circulates in the second medium flow channel 112 to indirectly exchange heat with the adsorbent, and the cooling gas circulates in the third flow channel 1133 to indirectly exchange heat with the adsorbent to cool the adsorbent.

[0036] In some embodiments, in order to extend the residence time of the gas in the regeneration tower 110 to achieve better heat exchange effect and improve energy utilization efficiency, at least one of the first flow channel 1113, the second flow channel 1123, and the third flow channel 1133 is a serpentine flow channel.

[0037] As an example, in the embodiment shown in FIG1 , a plurality of baffles 140 are respectively provided in the preheating section 111, the heating section 112, and the cooling section 113. The baffles 140 are arranged horizontally and spaced apart vertically, forming a serpentine first flow channel 1113, a serpentine second flow channel 1123, and a serpentine third flow channel 1133 in the preheating section 111, the heating section 112, and the cooling section 113, respectively. The provision of the serpentine first flow channel 1113, the serpentine second flow channel 1123, and the serpentine third flow channel 1133 prolongs the flow path and residence time of the gas therein, facilitates complete heat exchange of the gas, further improves energy utilization, and reduces the operating costs of the regeneration device.

[0038] In some embodiments, a regeneration inlet 115 is provided at the top of the regeneration tower 110 , and a regeneration outlet 116 is provided at the bottom of the regeneration tower 110 . The adsorbent to be regenerated enters the regeneration tower 110 from the regeneration inlet 115 , and the regenerated adsorbent is discharged from the regeneration outlet 116 .

[0039] As shown in Figure 1, the regeneration tower 110 is equipped with a plurality of first discharge pipes 1171, a plurality of second discharge pipes 1172, and a plurality of third discharge pipes 1173. The first discharge pipes 1171 are arranged in parallel in the preheating section 111 to form a first discharge layer, the second discharge pipes 1172 are arranged in parallel in the heating section 112 to form a second discharge layer, and the third discharge pipes 1173 are arranged in parallel in the cooling section 113 to form a third discharge layer. The first discharge pipes 1171, the second discharge pipes 1172, and the third discharge pipes 1173 all extend vertically to facilitate the drop of adsorbent. Adsorbent entering the regeneration inlet 115 flows sequentially through the first discharge pipes 1171, the second discharge pipes 1172, and the third discharge pipes 1173 before being discharged from the regeneration outlet 116. The vertically extending first, second, and third feed tubes 1171, 1172, and 1173 allow the adsorbent to descend smoothly, preventing clogging. Specifically, these tubes act as guides, directing the adsorbent's downward flow. Furthermore, within each feed layer, several first, second, and third feed tubes 1171, 1172, and 1173 are arranged in parallel, increasing the heat exchange area. This allows for efficient and uniform heat exchange between the adsorbent inside the tubes and the heat exchange medium outside, improving heat exchange efficiency and achieving excellent heat exchange results.

[0040] In the preheating section 111, a first flow channel 1113 is defined between the outer side of the first discharge pipe 1171 and the inner wall surface of the regeneration tower 110. In the heating section 112, a second flow channel 1123 is defined between the outer side of the second discharge pipe 1172 and the inner wall surface of the regeneration tower 110. In the cooling section 113, a third flow channel 1133 is defined between the outer side of the third discharge pipe 1173 and the inner wall surface of the regeneration tower 110.

[0041] In some embodiments, as shown in Figures 1 and 2, a distribution chamber for forming a distribution layer 1181 is provided below the regeneration inlet 115 and above the first discharge pipe 1171. The distribution layer 1181 is formed by the adsorbent entering the regeneration tower 110 from the regeneration inlet 115 and accumulating on top of the first discharge pipe 1171. The adsorbent entering the regeneration tower 110 from the regeneration inlet 115 first accumulates in the distribution layer 1181 and then enters and flows downwardly along the plurality of parallel first discharge pipes 1171. The formation of the distribution layer 1181 facilitates uniform distribution of the adsorbent throughout the plurality of first discharge pipes 1171, allowing the adsorbent to be naturally distributed within the plurality of first discharge pipes 1171.

[0042] The adsorbent in the material layer 1181 gradually falls into the first discharge pipe 1171. A first transition chamber is provided between the preheating section 111 and the heating section 112, forming a first material layer 1182. Specifically, the first material layer 1182 is formed between the first and second discharge layers. To prevent heat exchange medium from flowing between the heating section 112 and the preheating section 111, a partition separates the top of the first transition chamber from the first flow channel 1113, and a partition separates the bottom of the first transition chamber from the second flow channel 1123. Specifically, the first transition chamber is defined by two vertically spaced partitions, which are connected to the inner wall of the regeneration tower 110. It is understood that the bottom end of the first discharge pipe 1171 passes through the upper partition to communicate with the first transition chamber, while the top opening of the second discharge pipe 1172 passes through the lower partition to communicate with the first transition chamber, allowing smooth flow of adsorbent.

[0043] A second transition chamber for forming a second material layer 1183 is provided between the heating section 112 and the cooling section 113. Specifically, the second material layer 1183 is formed between the second lower material layer and the third lower material layer. Adsorbent desorption to produce regeneration gas primarily occurs in the second material layer 1183. To prevent heat exchange medium from flowing between the heating section 112 and the cooling section 113, a partition is provided between the top of the second transition chamber and the second flow channel 1123, and between the bottom of the second transition chamber and the third flow channel 1133. Specifically, the second transition chamber is defined by two vertically spaced partitions, which are connected to the inner wall of the regeneration tower 110. It is understood that the bottom end of the second material discharge pipe 1172 passes through the upper partition to communicate with the first transition chamber, while the top opening of the third material discharge pipe 1173 passes through the lower partition to communicate with the second transition chamber, allowing smooth flow of adsorbent.

[0044] After the adsorbent to be regenerated enters from the regeneration inlet 115, it accumulates to form a cloth layer 1181. The adsorbent in the cloth layer 1181 and the preheated adsorbent that falls into the first discharge pipe 1171 are in a heated state, and will undergo partial desorption to produce regeneration gas containing water vapor. This part of the regeneration gas is easy to agglomerate with the adsorbent to form material blocks with relatively large particles, causing the discharge pipe to be blocked.

[0045] In order to avoid the blockage problem caused by material agglomeration, in some embodiments, as shown in Figure 2, the cloth chamber is provided with a first suction port 1191 located above the cloth layer 1181, and the first suction port 1191 is used to promptly extract the regeneration gas generated in the preheating section 111 and the cloth layer 1181.

[0046] In some embodiments, as shown in FIG2 , the first transition chamber is provided with a second suction port 1192 for promptly extracting the regeneration gas to prevent the water vapor in the regeneration gas from causing the material to agglomerate.

[0047] In some embodiments, as shown in FIG2 , the second transition chamber is provided with a third suction port 1193 for promptly extracting the regeneration gas to prevent the water vapor in the regeneration gas from causing the material to agglomerate.

[0048] In some embodiments, in the preheating section 111, the mixed gas initially heats the adsorbent to 50 degrees Celsius to 110 degrees Celsius; in the heating section 112, the high-temperature air heats the adsorbent to 150 degrees Celsius to 350 degrees Celsius to desorb and regenerate the adsorbent; in the cooling section 113, the cooling gas cools the adsorbent to 50 degrees Celsius to 100 degrees Celsius.

[0049] In some specific embodiments, in the preheating section 111, the mixed gas preliminarily heats the adsorbent to 100 degrees Celsius; in the heating section 112, the high-temperature air heats the adsorbent to 300 degrees Celsius to desorb and regenerate the adsorbent; in the cooling section 113, the cooling gas cools the adsorbent to 80 degrees Celsius.

[0050] The second embodiment of the present disclosure provides a low-temperature adsorption regeneration system, which includes an adsorption tower and a regeneration system 100, wherein the regeneration system 100 is the regeneration system 100 in any embodiment of the first aspect.

[0051] The adsorption tower has a flue gas inlet and a flue gas outlet. Low-temperature flue gas below room temperature enters the adsorption tower from the flue gas inlet, comes into contact with the adsorbent for adsorption, and is converted into clean flue gas and discharged from the flue gas outlet. The regeneration system 100 is used to regenerate the adsorbent saturated with adsorption discharged from the adsorption tower and return the regenerated adsorbent to the adsorption tower. The adsorption tower also has a feed inlet and a discharge port. The regeneration outlet 116 of the regeneration system 100 is connected to the feed inlet of the adsorption tower, and the discharge port of the adsorption tower is connected to the regeneration inlet 115 of the regeneration system 100. The adsorbent saturated with adsorption is fed into the regeneration system 100 for regeneration.

[0052] In some embodiments, the temperature of the low-temperature flue gas is below zero, for example, -80°C to -5°C.

[0053] In some embodiments, the temperature of the low-temperature flue gas is -20°C to -5°C. The inventors have discovered through research that the lower the flue gas temperature, the more beneficial it is for adsorption purification. However, too low a flue gas temperature complicates the structure of the flue gas cooling equipment and increases energy consumption. For example, insulation layers are required for the cooling equipment, adsorption tower, and pipelines, requiring high sealing performance, which increases costs. Furthermore, excessively low temperatures can easily lead to condensation in the adsorption tower, causing the adsorbent to stick and clog, affecting adsorption. Therefore, cooling the flue gas to a temperature of -20°C to -5°C is advantageous.

[0054] Since the clean flue gas discharged from the adsorption tower's flue gas outlet is relatively low in temperature, a large amount of available cooling capacity remains. To fully utilize the cooling capacity in the low-temperature flue gas, in some embodiments, the flue gas outlet is connected to the cooling inlet 1131 of the cooling section 113. The clean flue gas output from the flue gas outlet is fed into the cooling section 113 as cooling gas to indirectly cool the adsorbent within the cooling section 113.

[0055] In the description of the present disclosure, 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 disclosure 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 to the present disclosure.

[0056] 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 technical features being referred to. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. Throughout the present disclosure, "plurality" means at least two, such as two, three, etc., unless otherwise specifically defined.

[0057] In this disclosure, unless otherwise expressly specified or limited, terms such as "mounted," "connected," "connect," and "fixed" should be understood in a broad sense. For example, they may refer to fixed connections, detachable connections, or integration; mechanical connections, electrical connections, or communication between them; direct connections or indirect connections through an intermediate medium; and internal communication between two elements or interaction between two elements, unless otherwise expressly limited. Those skilled in the art will understand the specific meanings of the above terms in this disclosure based on specific circumstances.

[0058] In the present disclosure, 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.

[0059] In the present disclosure, 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 disclosure. In this specification, the schematic expressions 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 features of different embodiments or examples without contradiction.

[0060] Although the embodiments of the present disclosure have been shown and described above, it is understood that the above embodiments are illustrative and are not to be construed as limitations on the present disclosure. A person skilled in the art may change, modify, replace and vary the above embodiments within the scope of the present disclosure.

Claims

1. A regeneration device coupled with flue gas waste heat recovery, characterized in that Comprising: A regeneration tower, which is divided from top to bottom into a preheating section for preheating the adsorbent, a heating section for heating the preheated adsorbent to regenerate and desorb the adsorbent, and a cooling section for cooling the regenerated adsorbent. The preheating section is provided with a preheating inlet and a preheating outlet, the heating section is provided with a heating inlet and a heating outlet, the cooling section is provided with a cooling inlet and a cooling outlet, and the cooling inlet is used for supplying cooling gas into the cooling section to cool the adsorbent; An air preheater, the hot side inlet of the air preheater is communicated with the flue gas outlet of the economizer, the cold side inlet of the air preheater is communicated with the blower, the cold side outlet of the air preheater is communicated with the heating inlet. The flue gas input from the economizer into the air preheater exchanges heat with the gas input from the blower into the air preheater to heat the gas input from the blower into the air preheater into high-temperature air and then input it into the heating section through the heating inlet. The cooling outlet is communicated with the heating outlet and the preheating inlet, so that the cooling gas discharged from the cooling section and the air discharged from the heating outlet are mixed into a mixed gas and then enter the preheating section to preheat the adsorbent in the preheating section.

2. The regeneration device for coupling flue gas waste heat recovery according to claim 1, wherein The ratio of the cooling gas supplied from the cooling outlet to the preheating inlet to the air supplied from the heating outlet to the preheating inlet is adjustable to adjust the temperature of the mixed gas.

3. The regenerative device for coupling flue gas waste heat recovery according to claim 1 or 2, characterized in that, A first flow channel for flowing the mixed gas is provided in the preheating section, a second flow channel for flowing the high-temperature air is provided in the heating section, and a third flow channel for flowing the cooling gas is provided in the cooling section. At least one of the first flow channel, the second flow channel, and the third flow channel is a serpentine flow channel.

4. The regeneration device for coupling flue gas waste heat recovery according to claim 3, wherein A plurality of horizontally arranged baffles are provided in the regeneration tower, and the plurality of baffles are spaced apart in the vertical direction to define the serpentine first flow channel, the serpentine second flow channel, and the serpentine third flow channel.

5. The regeneration device for coupling flue gas waste heat recovery according to any one of claims 1 to 4, characterized in that The preheating section is provided with a plurality of first blanking pipes, the heating section is provided with a plurality of second blanking pipes, and the cooling section is provided with a plurality of third blanking pipes. The first blanking pipes, the second blanking pipes, and the third blanking pipes all extend in the vertical direction and are used for the falling of the adsorbent.

6. The regeneration device for coupling flue gas waste heat recovery according to claim 5, characterized in that, A cloth cavity for forming a cloth layer is provided above the first blanking pipe. A first transition cavity for forming a first stockpiling layer is provided between the preheating section and the heating section. A second transition cavity for forming a second stockpiling layer is provided between the heating section and the cooling section. The cloth cavity is provided with a first suction port above the cloth layer.

7. The regeneration device for coupling flue gas waste heat recovery according to claim 6, characterized in that, The first transition cavity is provided with a second suction port, and / or the second transition cavity is provided with a third suction port.

8. The regeneration device for coupling flue gas waste heat recovery according to any one of claims 1 to 7, characterized in that In the preheating section, the mixed gas preheats the adsorbent to 50 °C - 110 °C; In the heating section, the high-temperature air heats the adsorbent to 150 °C - 350 °C; In the cooling section, the cooling gas cools the adsorbent to 50 °C - 100 °C.

9. A low-temperature adsorption regeneration system, characterized in that, Comprising: An adsorption tower, the adsorption tower having a flue gas inlet and a flue gas outlet, low-temperature flue gas below room temperature enters the adsorption tower from the flue gas inlet and contacts the adsorbent to be adsorbed and purified by the adsorbent into clean flue gas and discharged from the flue gas outlet; A regeneration device, the regeneration device being a regeneration device for coupling flue gas waste heat recovery according to any one of claims 1 to 8, the adsorbent saturated with adsorption discharged from the adsorption tower is regenerated in the regeneration device and the regenerated adsorbent is transported back to the adsorption tower.

10. The cryogenic adsorption regeneration system according to claim 9, characterized in that, The flue gas outlet is communicated with the cooling inlet, and the clean flue gas output from the flue gas outlet is input into the cooling section as the cooling gas to indirectly cool the adsorbent in the cooling section.

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