Regeneration tower and flue gas low-temperature adsorption regeneration system

Abstract

The invention relates to the field of flue gas purification and discloses a regeneration tower and a flue gas low-temperature adsorption regeneration system. The regeneration tower comprises a tower body and a heating device, the tower body is divided into a preheating section used for preheating an adsorbent, a heating section used for heating the preheated adsorbent to desorb and regenerate the adsorbent and a cooling section used for cooling the regenerated adsorbent which are sequentially arranged from top to bottom, and the heating section is provided with a regenerated gas outlet used for discharging regenerated gas; the cooling outlet of the cooling section is communicated with the preheating inlet of the preheating section, so that the heat exchange medium which exchanges heat with the adsorbent in the cooling section in the cooling section is supplied into the preheating section to preheat the adsorbent in the preheating section. The heating device is arranged between the heating inlet and the heating outlet and used for heating the heat exchange medium output from the heating outlet and then inputting the heat exchange medium into the heating section. According to the regeneration tower provided by the invention, energy is fully utilized, and the energy consumption is effectively reduced.

Description

Technical Field

[0001] The invention relates to the technical field of flue gas purification, in particular to a regeneration tower and a flue gas low-temperature adsorption regeneration system. Background Art

[0002] In the related art, the coal-fired flue gas is passed into an adsorption tower filled with adsorbent to purify the coal-fired flue gas by adsorption, and the adsorbent saturated with adsorption enters the regeneration tower for heating and regeneration. In the related art, the adsorption of pollutants in the flue gas is usually carried out under high temperature environment, that is, the flue gas discharged from the boiler is cooled to about 200°C through a cooling tower, and then enters the adsorption tower for high temperature and adsorption purification. However, the adsorption of high-temperature flue gas has poor adsorption effect, and the content of nitrogen oxides in the clean flue gas after adsorption is high, and it is impossible to achieve near-zero emissions.

[0003] 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 a low-temperature flue gas below room temperature, for example, and the pollutants in the flue gas are adsorbed and removed from the flue gas by the adsorbent. In low-temperature adsorption, the adsorption capacity of the adsorbent is increased exponentially in a low-temperature environment, which greatly improves the adsorption purification rate compared with the conventional high-temperature flue gas adsorption, and can achieve near-zero flue gas emissions. However, the inventors have realized through research that in the high-temperature adsorption tower, due to heat exchange with the high-temperature flue gas, the adsorbent saturated with adsorption discharged has a high temperature (above 180°C). This high-temperature adsorbent is transported to the regeneration tower, and the heating load of heating to the regeneration temperature (250°C-350°C) is small, and the traditional one-stage heating method can meet the heating requirements. In the low-temperature adsorption process, the adsorbent is in contact with the low-temperature flue gas, resulting in a low discharge temperature (for example, below room temperature). The conventional one-stage heating regeneration tower is used to heat and regenerate the adsorbent. The load of the heater is large, and the regeneration energy consumption and cost remain high, which affects the further development of the low-temperature flue gas adsorption technology. Summary of the invention

[0004] The present invention is based on the inventor's discovery and understanding of the following facts and problems:

[0005] The related art proposes a technical solution that the regeneration tower is divided into a preheating section, a heating section and a cooling section from top to bottom, and the heat exchange medium output from the cooling section is input into the preheating section to preheat the adsorbent, the heat exchange medium output from the preheating section is heated by the heat exchanger of the boiler and then input into the heating section to heat the adsorbent, and the heat exchange medium output from the heating section is mixed with hot air and then returned to the boiler. However, the inventors found that the technical solution has the following problems: In the low-temperature adsorption technology, since the temperature of the adsorbent input into the preheating section is relatively low (usually below room temperature), the temperature of the heat exchange medium output from the preheating section is not high (usually 60°C - 80℃), it can be seen that there is less heat with usable value in this part of the heat exchange medium. The heat exchange medium output from the preheating section is input into the heat exchanger of the boiler system for heat exchange and temperature increase with the high-temperature flue gas, and then input into the heating section. The transformation is difficult, the pipeline is long, and the cost is high. Therefore, it is not cost-effective in practical applications; in addition, the temperature of the heat exchange medium output from the heating section is generally around 200℃-220℃, while the temperature of the hot air returned to the furnace is generally above 260℃. If the two are mixed and input into the boiler, it will affect the operating conditions of the boiler to a certain extent, and have a certain impact on the normal operation of the boiler.

[0006] The present invention aims to solve one of the technical problems in the related art at least to a certain extent. To this end, the present invention proposes a regeneration tower.

[0007] An embodiment of the present invention further provides a flue gas low-temperature adsorption regeneration system.

[0008] The regeneration tower provided by the present invention comprises: a tower body, wherein the tower body is divided into a preheating section, a heating section and a cooling section arranged in sequence from top to bottom, the heating section is provided with a regeneration gas outlet for discharging the regeneration gas, the preheating section has a preheating inlet for supplying a heat exchange medium into the preheating section to preheat an adsorbent and a preheating outlet for discharging the heat exchange medium in the preheating section, the heating section has a heating inlet for supplying a heat exchange medium into the heating section to heat the adsorbent and a heating outlet for discharging the heat exchange medium in the heating section, the cooling section has a heating inlet for supplying a heat exchange medium into the cooling section to cool the adsorbent A cooling inlet for the adsorbent and a cooling outlet for discharging the heat exchange medium in the cooling section, wherein the cooling outlet of the cooling section is connected to the preheating inlet of the preheating section so that the heat exchange medium that has exchanged heat with the adsorbent in the cooling section in the cooling section is supplied to the preheating section to preheat the adsorbent in the preheating section; a heating device, which is arranged between the heating inlet and the heating outlet and is used to heat the heat exchange medium output from the heating outlet and then input it into the heating section to indirectly heat the adsorbent in the heating section through heat exchange to desorb and regenerate the adsorbent in the heating section.

[0009] The regeneration tower provided by the present invention 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. This multi-stage heating regeneration method realizes the step-by-step recycling of energy, reduces the temperature rise range of the adsorbent in the heating section, effectively alleviates the heating load of the heater, reduces the energy consumption of the regeneration system, and reduces the operating cost of the regeneration system. The multi-stage heating regeneration method of the adsorbent is conducive to increasing the residence time of the adsorbent in the regeneration tower, so that the regeneration of the adsorbent is more thorough. In addition, the setting of the cooling section allows the adsorbent to be cooled to a certain extent before leaving the tower, and 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, and helps to improve the adsorption efficiency of the adsorption tower.

[0010] In addition, since the heat exchange medium output from the cooling section has a certain amount of heat (generally 150°C-250°C) in the heat exchange zone with the adsorbent, the present invention makes full use of this heat and inputs the heat exchange medium output from the cooling section into the preheating section to preheat the adsorbent. The preheating section does not require other heat sources, fully utilizes energy, and effectively reduces energy consumption. The heat exchange medium discharged from the preheating outlet of the preheating section is directly emptied and no longer input into the boiler for reuse, which reduces the number and length of pipelines, and reduces the equipment construction cost and equipment complexity. In addition, the heating section performs self-circulation of the heat exchange medium. The heat of the heating section comes from the heating device, and there is no need to couple with the boiler system, which reduces the number and length of pipelines, making the regeneration tower relatively independent, while also avoiding situations that affect the operation of the boiler.

[0011] Optionally, the adsorbent is preheated to 80°C-150°C in the preheating section, and / or the adsorbent is heated to 250°C-350°C in the heating section, and / or the adsorbent is cooled to 50°C-100°C in the cooling section.

[0012] Optionally, the temperature of the heat exchange medium discharged from the cooling outlet is 150°C-250°C, and the temperature of the heat exchange medium discharged from the preheating outlet is 50°C-80°C.

[0013] Optionally, the temperature of the heat exchange medium discharged from the heating outlet is 200°C-250°C.

[0014] Optionally, the heating device is an electric heater; or, the heating device is a heat exchanger, the cold side inlet of the heat exchanger is connected to the cooling inlet of the cooling section, the cold side outlet of the heat exchanger is connected to the heating inlet of the heating section, and the heat exchanger is connected to the economizer to utilize the high-temperature flue gas output by the economizer to heat the heat exchange medium on the cold side of the heat exchanger.

[0015] Optionally, a plurality of first discharge pipes are provided in the preheating section, a plurality of second discharge pipes are provided in the heating section, and a plurality of third discharge pipes are provided in the cooling section, and the first discharge pipe, the second discharge pipe and the third discharge pipe all extend in a vertical direction and are used for the dropping of the adsorbent; a material distribution cavity for forming a material distribution layer is provided above the first discharge pipe, a first transition cavity for forming a first material stacking layer is provided between the preheating section and the heating section, a second transition cavity for forming a second material stacking layer is provided between the heating section and the cooling section, and the regeneration gas outlet is connected to the second transition cavity.

[0016] Optionally, the fabric cavity is provided with a first suction port located above the fabric layer, and the first transition cavity is provided with a second suction port.

[0017] The present invention also proposes a flue gas low-temperature adsorption regeneration system, 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 with an adsorbent so that the low-temperature flue gas is adsorbed and purified into clean flue gas and discharged from the flue gas outlet; a regeneration tower, the regeneration tower is used to regenerate the adsorption saturated adsorbent discharged from the adsorption tower and the regenerated adsorbent is returned to the adsorption tower.

[0018] Optionally, the flue gas outlet is communicated with a cooling inlet of the cooling section, so that the clean flue gas outputted from the flue gas outlet is inputted into the cooling section to indirectly cool the adsorbent in the cooling section. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a structural schematic diagram of a regeneration tower provided in an embodiment of the present invention.

[0020] Figure 2 It is a schematic diagram of the internal structure of the regeneration tower provided in an embodiment of the present invention.

[0021] Reference numerals:

[0022] Regeneration tower 100, tower body 110, preheating section 111, preheating inlet 1111, preheating outlet 1112, first medium flow channel 1113, heating section 112, heating inlet 1121, heating outlet 1122, second medium flow channel 1123, cooling section 113, cooling inlet 1131, cooling outlet 1132, third medium flow channel 1133, regeneration inlet 115, regeneration outlet 116, first feed pipe 1171, second feed pipe 1172, third feed pipe 1173, material distribution layer 1181, first material stacking layer 1182, second material stacking layer 1183, first suction port 1191, second suction port 1192, regeneration gas outlet 1193, pipeline 120, electric heater 130, heating pipe 140, fan 150, partition 160. DETAILED DESCRIPTION

[0023] Embodiments of the present invention 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 invention, but should not be understood as limiting the present invention.

[0024] According to the following Figure 1 and Figure 2 The regeneration tower 100 proposed in the embodiment of the present invention is described, and the regeneration tower 100 includes a tower body 110 and a temperature increasing device 130. The tower body 110 is divided into a preheating section 111, a heating section 112 and a cooling section 113 from top to bottom, and the adsorbent passes through the preheating section 111, the heating section 112 and the cooling section 113 from top to bottom. The preheating section 111 is used for preheating the adsorbent, and the heating section 112 is used for heating the preheated adsorbent to desorb and regenerate the adsorbent. The cooling section 113 is used to cool the regenerated adsorbent. The heating section 112 is provided with a regeneration gas outlet 1193 for discharging the regeneration gas.

[0025] The preheating section 111 has a preheating inlet 1111 for supplying heat exchange medium into the preheating section 111 to preheat the adsorbent and a preheating outlet 1112 for discharging the heat exchange medium in the preheating section 111. The heating section 112 has a heating inlet 1121 for supplying heat exchange medium into the heating section 112 to heat the adsorbent and a heating outlet 1122 for discharging the heat exchange medium in the heating section 112. The cooling section 113 is correspondingly provided with a cooling inlet 1131 for supplying heat exchange medium into the cooling section 113 to cool the adsorbent and a cooling outlet 1132 for discharging the heat exchange medium in the cooling section 113. The cooling outlet 1132 of the cooling section 113 is connected to the preheating inlet 1111 of the preheating section 111 through the pipeline 120, so that the heat exchange medium after heat exchange with the adsorbent in the cooling section 113 in the cooling section 113 is supplied to the preheating section 111 to preheat the adsorbent in the preheating section 111.

[0026] The low-temperature heat exchange medium enters the cooling section 113 from the cooling inlet 1131 to cool the adsorbent, and the heat exchange medium after heat exchange flows out of the cooling section 113 from the cooling outlet 1132. The heat exchange medium flowing out of the cooling section 113 carries a large amount of heat, and the heat exchange medium enters the preheating section 111 through the pipeline 120 to indirectly preheat the adsorbent in the preheating section 111 by heat exchange, and the heat exchange medium after heat release is discharged from the preheating section 111 from the preheating outlet 1112.

[0027] like Figure 1 As shown, the temperature increasing device 130 is arranged between the heating inlet 1121 and the heating outlet 1122. The temperature increasing device 130 is used to heat the heat exchange medium output from the heating outlet 1122 and then input it into the heating section 112 to indirectly heat the adsorbent in the heating section 112 through heat exchange to desorb and regenerate the adsorbent in the heating section 112.

[0028] For the adsorbent, the adsorbent circulates from top to bottom and undergoes preheating, heating regeneration and cooling in sequence. Specifically, the heat exchange medium preliminarily heats the adsorbent entering the regeneration tower 110 in the preheating section 111, i.e., preheats it. The heat exchange medium further heats the preheated adsorbent in the heating section 112 to completely desorb the pollutants adsorbed by the adsorbent. The heat exchange medium cools the regenerated adsorbent after desorption in the cooling section 113. It can be understood that the temperature of the heat exchange medium in the heating section 112 is higher than the temperature of the heat exchange medium in the preheating section 111.

[0029] The regeneration tower provided by the present invention 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. This multi-stage heating regeneration method realizes the step-by-step recycling of energy, reduces the temperature rise range of the adsorbent in the heating section, effectively alleviates the heating load of the electric heater, reduces the energy consumption of the regeneration system, and reduces the operating cost of the regeneration system. The multi-stage heating regeneration method of the adsorbent is conducive to increasing the residence time of the adsorbent in the regeneration tower, so that the regeneration of the adsorbent is more thorough. In addition, the setting of the cooling section allows the adsorbent to be cooled to a certain extent before leaving the tower, and 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, and helps to improve the adsorption efficiency of the adsorption tower.

[0030] In addition, since the heat exchange medium output from the cooling section has a certain amount of heat (generally 150°C-250°C) in the heat exchange zone with the adsorbent, the present invention makes full use of this heat and inputs the heat exchange medium output from the cooling section into the preheating section to preheat the adsorbent. The preheating section does not require other heat sources, fully utilizes energy, and effectively reduces energy consumption. The heat exchange medium discharged from the preheating outlet of the preheating section is directly emptied and no longer input into the boiler for reuse, which reduces the number and length of pipelines, and reduces the equipment construction cost and equipment complexity. In addition, the heating section performs self-circulation of the heat exchange medium. The heat of the heating section comes from the heating device, and there is no need to couple with the boiler system, which reduces the number and length of pipelines, making the regeneration tower relatively independent, while also avoiding situations that affect the operation of the boiler.

[0031] Optionally, the heat exchange medium flowing in the regeneration tower 110 may be gas or liquid.

[0032] Preferably, in order to reduce operating costs, the heat exchange medium flowing through the regeneration tower 100 is air.

[0033] Specifically, Figure 1As shown, room temperature air enters the cooling section 113 from the cooling inlet 1131, and the air discharged from the preheating outlet 1112 is directly discharged. A fan 150 is connected to the heating pipe 140 to drive the hot air in the heating circuit so that the air circulates in the heating circuit.

[0034] In some embodiments, in the preheating section 111, the heat exchange medium preliminarily heats the adsorbent to 80 degrees Celsius-110 degrees Celsius; in the heating section 112, the heat exchange medium heats the adsorbent to 250 degrees Celsius-350 degrees Celsius to desorb and regenerate the adsorbent; in the cooling section 113, the heat exchange medium cools the adsorbent to 50 degrees Celsius-100 degrees Celsius.

[0035] In some specific embodiments, in the preheating section 111, the heat exchange medium preliminarily heats the adsorbent to 100 degrees Celsius; in the heating section 112, the heat exchange medium heats the adsorbent to 300 degrees Celsius to desorb and regenerate the adsorbent; in the cooling section 113, the heat exchange medium cools the adsorbent to 80 degrees Celsius.

[0036] Optionally, the temperature of the heat exchange medium discharged from the cooling outlet 1132 of the cooling section 113 is 150° C.-250° C. The temperature of the heat exchange medium discharged from the preheating outlet 1112 is 50° C.-80° C.

[0037] Optionally, the temperature of the heat exchange medium discharged from the heating outlet is 200°C-250°C.

[0038] In some optional embodiments, such as Figure 1 As shown, the temperature increasing device 130 is an electric heater, which is arranged on the heating pipe 140, and the heating pipe 140 is connected to the heating inlet 1121 and the heating outlet 1122. The electric heater is used to heat the heat exchange medium output from the cooling outlet 1132 and then input it into the heating section 112 to indirectly heat the adsorbent in the heating section 112 through heat exchange to desorb and regenerate the adsorbent in the heating section 112.

[0039] In some alternative embodiments, the temperature increasing device 130 may be a heat exchanger, the cold side inlet of the heat exchanger is connected to the heating outlet 1122, the cold side outlet of the heat exchanger is connected to the heating inlet 1121, and the heat exchanger is connected to the economizer to heat the heat exchange medium on the cold side of the heat exchanger using the high temperature flue gas output by the economizer. In other words, the hot side inlet of the heat exchanger is connected to the high temperature flue gas outlet of the economizer, the high temperature flue gas is input to the hot side of the heat exchanger, and heat is exchanged with the heat exchange medium on the cold side of the heat exchanger to heat the heat exchange medium, and the heated heat exchange medium is input into the heating section 112 to heat the adsorbent in the regeneration heating section 112.

[0040] In some embodiments, Figure 2As shown, the preheating section 111 has a first medium flow channel 1113 for circulating heat exchange medium, the first medium flow channel 1113 connects the preheating inlet 1111 and the preheating outlet 1112, the heating section 112 has a second medium flow channel 1123 for circulating heat exchange medium, the second medium flow channel 1123 connects the heating inlet 1121 and the heating outlet 1122, and the cooling section 113 has a third medium flow channel 1133 for circulating heat exchange medium, the third medium flow channel 1133 connects the cooling inlet 1131 and the cooling outlet 1132. The heat exchange medium circulates in the first medium flow channel 1113 to indirectly exchange heat with the adsorbent to preheat the adsorbent, the heat exchange medium circulates in the second medium flow channel 112 to indirectly exchange heat with the adsorbent to heat the adsorbent so as to regenerate the adsorbent, and the heat exchange medium circulates in the third medium flow channel 1133 to indirectly exchange heat with the adsorbent to cool the adsorbent.

[0041] Preferably, in order to extend the residence time of the heat exchange medium in the regeneration tower 110 to achieve a better heat exchange effect and improve energy utilization efficiency, at least one of the first medium flow channel 1113, the second medium flow channel 1123, and the third medium flow channel 1133 is a serpentine flow channel. The arrangement of the serpentine first medium flow channel 1113, the serpentine second medium flow channel 1123, and the serpentine third medium flow channel 1133 extends the flow path and residence time of the heat exchange medium therein, helps complete heat exchange of the heat exchange medium, can further improve energy utilization, and reduce the operating cost of the regeneration device.

[0042] As an example, in Figure 2 In the illustrated embodiment, a plurality of partitions 160 are respectively provided in the preheating section 111, the heating section 112 and the cooling section 113. The partitions 160 are horizontally arranged and spaced apart in the vertical direction to form a serpentine first medium flow channel 1113, a serpentine second medium flow channel 1123 and a serpentine third medium flow channel 1133 in the preheating section 111, the heating section 112 and the cooling section 113, respectively.

[0043] 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 .

[0044] like Figure 2As shown, a plurality of first feed pipes 1171, a plurality of second feed pipes 1172 and a plurality of third feed pipes 1173 are provided in the regeneration tower 110. The first feed pipes 1171 are arranged in parallel in the preheating section 111 to form a first feed layer, the second feed pipes 1172 are arranged in parallel in the heating section 112 to form a second feed layer, and the third feed pipes 1173 are arranged in parallel in the cooling section 113 to form a third feed layer. The first feed pipes 1171, the second feed pipes 1172 and the third feed pipes 1173 all extend in a vertical direction for the adsorbent to fall. The adsorbent entering from the regeneration inlet 115 flows through the first feed pipe 1171, the second feed pipe 1172 and the third feed pipe 1173 in sequence and is discharged from the regeneration outlet 116. The first feed pipe 1171, the second feed pipe 1172 and the third feed pipe 1173 extending in the vertical direction allow the adsorbent to fall smoothly and avoid adsorbent blockage, that is, the first feed pipe 1171, the second feed pipe 1172 and the third feed pipe 1173 play a guiding role, guiding the adsorbent to flow from top to bottom. In each feed layer, a plurality of first feed pipes 1171, a plurality of second feed pipes 1172 and a plurality of third feed pipes 1173 are arranged in parallel, respectively, which can increase the heat exchange area, so that the adsorbent inside the feed pipe and the heat exchange medium outside can achieve effective and uniform heat exchange, improve the heat exchange efficiency, and achieve excellent heat exchange effect.

[0045] In the preheating section 111, a first medium flow channel 1113 is defined between the outer side of the first feed pipe 1171 and the inner wall surface of the regeneration tower 110. In the heating section 112, a second medium flow channel 1123 is defined between the outer side of the second feed pipe 1172 and the inner wall surface of the regeneration tower 110. In the cooling section 113, a third medium flow channel 1133 is defined between the outer side of the third feed pipe 1173 and the inner wall surface of the regeneration tower 110.

[0046] Furthermore, if Figure 2 As shown, a distribution cavity for forming a distribution layer 1181 is provided below the regeneration inlet 115 and above the first feed pipe 1171. The distribution layer 1181 is formed by the adsorbent entering the regeneration tower 110 from the regeneration inlet 115 and accumulating on the top of the first feed pipe 1171. The adsorbent entering the regeneration tower 110 from the regeneration inlet 115 is first accumulated in the distribution layer 1181, and then enters a plurality of parallel first feed pipes 1171 and flows downward along the first feed pipes 1171. The formation of the distribution layer 1181 helps to evenly distribute the adsorbent in the plurality of first feed pipes 1171, so that the adsorbent can be naturally distributed to the plurality of first feed pipes 1171.

[0047] The adsorbent in the cloth layer 1181 gradually falls into the first discharge pipe 1171. A first transition chamber for forming a first material layer 1182 is provided between the preheating section 111 and the heating section 112, that is, a first material layer 1182 is formed between the first discharge layer and the second discharge layer. In order to prevent the heat exchange medium from flowing between the regeneration section 112 and the preheating section 111, the top of the first transition chamber is isolated from the first medium flow channel 1113 by a partition, and the bottom of the first transition chamber is isolated from the second medium flow channel 1123 by a partition, that is, the first transition chamber is defined by two partitions spaced apart in the vertical direction, and the partition is connected to the inner wall surface of the regeneration tower 110. It can be understood that the bottom end of the first discharge pipe 1171 is connected to the first transition chamber through the upper partition, and the top opening of the second discharge pipe 1172 is connected to the first transition chamber through the lower partition, so that the adsorbent can flow smoothly.

[0048] A second transition chamber for forming a second material layer 1183 is provided between the heating section 112 and the cooling section 113, that is, a second material layer 1183 is formed between the second lower material layer and the third lower material layer. The regeneration gas outlet 1193 is connected to the second transition chamber. The desorption of the adsorbent to produce regeneration gas mainly occurs in the second material layer 1183. In order to prevent the heat exchange medium from flowing between the regeneration section 112 and the cooling section 113, the top of the second transition chamber is isolated from the second medium flow channel 1123 by a partition, and the bottom of the second transition chamber is isolated from the third medium flow channel 1133 by a partition, that is, the second transition chamber is defined by two partitions spaced apart in the vertical direction, and the partition is connected to the inner wall surface of the regeneration tower 110. It can be understood that the bottom end of the second material discharge pipe 1172 is connected to the first transition chamber through the upper partition, and the top opening of the third material discharge pipe 1173 is connected to the second transition chamber through the lower partition, so that the adsorbent can flow smoothly.

[0049] 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, which causes the discharge pipe to be blocked.

[0050] In order to avoid the blockage problem caused by material agglomeration, in some embodiments, as Figure 2 As shown, 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 timely extract the regeneration gas generated in the preheating section 111 and the cloth layer 1181 .

[0051] In some embodiments, Figure 2As shown, the first transition chamber is provided with a second suction port 1192 for timely extracting the regeneration gas to prevent the water vapor in the regeneration gas from causing the material to agglomerate.

[0052] Another embodiment of the present invention further provides a flue gas low temperature adsorption regeneration system. The flue gas low temperature adsorption regeneration system comprises an adsorption tower and a regeneration tower 100, wherein the regeneration tower 100 is the regeneration tower 100 in any of the above embodiments.

[0053] 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 and contacts with the adsorbent for adsorption, and becomes clean flue gas and is discharged from the flue gas outlet. The regeneration tower 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 tower 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 tower 100, so that the adsorbent saturated with adsorption is sent to the regeneration tower 100 for regeneration.

[0054] Preferably, the temperature of the low-temperature flue gas is below zero, for example, -80°C to -5°C.

[0055] More preferably, the temperature of the low-temperature flue gas is -20°C to -5°C. The inventors have found through research that the lower the flue gas temperature, the more beneficial it is for adsorption purification. However, if the flue gas temperature is too low, the equipment structure for cooling the flue gas will be complicated and the energy consumption will increase. For example, it is required to set up an insulation layer for the cooling equipment, adsorption tower and pipeline, and the sealing requirements are high, which will increase the cost. In addition, too low temperature conditions will easily cause condensation water to appear in the adsorption tower, causing the adsorbent to stick and clog, affecting the adsorption. Therefore, it is beneficial to cool the flue gas temperature to -20°C to -5°C.

[0056] Since the temperature of the clean flue gas discharged from the flue gas outlet of the adsorption tower is relatively low, there is still a large amount of available cold energy. In order to fully utilize the cold energy 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, and the clean flue gas output from the flue gas outlet is input into the cooling section 113 as a heat exchange medium to indirectly cool the adsorbent in the cooling section 113.

[0057] In the description of the present invention, it is to 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”, etc., indicating orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0058] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0059] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral one; it can be a mechanical connection, an electrical connection, or communication with each other; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0060] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature 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. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0061] In the present invention, the terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" etc. 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 invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the described specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0062] Although the embodiments of the present invention have been shown and described above, it is to be understood that the above embodiments are exemplary and are not to be construed as limitations of the present invention. A person skilled in the art may change, modify, replace and vary the above embodiments within the scope of the present invention.

Claims

1. A regeneration tower, characterized in that: include: A tower body, wherein the tower body is divided into a preheating section, a heating section and a cooling section which are arranged in sequence from top to bottom, the heating section is provided with a regeneration gas outlet for discharging the regeneration gas, the preheating section has a preheating inlet for supplying a heat exchange medium into the preheating section to preheat an adsorbent and a preheating outlet for discharging the heat exchange medium in the preheating section, the heating section has a heating inlet for supplying a heat exchange medium into the heating section to heat an adsorbent and a heating outlet for discharging the heat exchange medium in the heating section, the cooling section has a cooling inlet for supplying a heat exchange medium into the cooling section to cool the adsorbent and a cooling outlet for discharging the heat exchange medium in the cooling section, wherein the cooling outlet of the cooling section is communicated with the preheating inlet of the preheating section, so that the heat exchange medium after heat exchange with the adsorbent in the cooling section in the cooling section is supplied to the preheating section to preheat the adsorbent in the preheating section; A heating device is provided between the heating inlet and the heating outlet, and is used for heating the heat exchange medium output from the heating outlet and then inputting it into the heating section, wherein the heated heat exchange medium indirectly heats the adsorbent in the heating section through heat exchange in the heating section so as to desorb and regenerate the adsorbent in the heating section.

2. The regeneration tower according to claim 1, characterized in that: The adsorbent is preheated to 80°C-150°C in the preheating section, and / or the adsorbent is heated to 250°C-350°C in the heating section, and / or the adsorbent is cooled to 50°C-100°C in the cooling section.

3. The regeneration tower according to claim 2, characterized in that: The temperature of the heat exchange medium discharged from the cooling outlet is 150°C-250°C, and the temperature of the heat exchange medium discharged from the preheating outlet is 50°C-80°C.

4. The regeneration tower according to any one of claims 1 to 3, characterized in that: The temperature of the heat exchange medium discharged from the heating outlet is 200°C-250°C.

5. The regeneration tower according to claim 1, characterized in that: The temperature increasing device is an electric heater.

6. The regeneration tower according to claim 1, characterized in that: The heating device is a heat exchanger, the cold side inlet of the heat exchanger is connected to the cooling inlet of the cooling section, the cold side outlet of the heat exchanger is connected to the heating inlet of the heating section, and the heat exchanger is connected to the economizer to use the high-temperature flue gas output by the economizer to heat the heat exchange medium on the cold side of the heat exchanger.

7. The regeneration tower according to claim 1, characterized in that: A plurality of first feed pipes are provided in the preheating section, a plurality of second feed pipes are provided in the heating section, and a plurality of third feed pipes are provided in the cooling section. The first feed pipes, the second feed pipes and the third feed pipes all extend in a vertical direction and are used for the adsorbent to fall. A material distribution cavity for forming a material distribution layer is provided above the first material discharge pipe, a first transition cavity for forming a first material stacking layer is provided between the preheating section and the heating section, a second transition cavity for forming a second material stacking layer is provided between the heating section and the cooling section, and the regeneration gas outlet is connected to the second transition cavity.

8. The regeneration tower according to claim 7, characterized in that: The fabric cavity is provided with a first suction port located above the fabric layer, and the first transition cavity is provided with a second suction port.

9. A flue gas low temperature adsorption regeneration system, characterized in that: include: An adsorption tower, wherein the adsorption tower has a flue gas inlet and a flue gas outlet, and 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 into clean flue gas and is discharged from the flue gas outlet; A regeneration tower, wherein the regeneration tower is a regeneration tower according to any one of claims 1 to 8, and the regeneration tower is used to regenerate the adsorbent saturated with adsorption discharged from the adsorption tower and return the regenerated adsorbent to the adsorption tower.

10. The flue gas low temperature adsorption regeneration system according to claim 9, characterized in that: The flue gas outlet is communicated with the cooling inlet of the cooling section, so that the clean flue gas outputted from the flue gas outlet is inputted into the cooling section to indirectly cool the adsorbent in the cooling section.

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