Flue gas coupling regeneration system and low-temperature flue gas adsorption system

Abstract

The invention relates to the field of flue gas purification and discloses a flue gas coupling regeneration system and a low-temperature flue gas adsorption system. The regeneration system comprises a regeneration tower, a heat exchanger, a heating device and a heating outer pipe. High-temperature flue gas input into the heat exchanger from the economizer exchanges heat with a heat exchange medium on the cold side of the heat exchanger so as to heat the heat exchange medium and then input the heated heat exchange medium into the first medium flow channel to preheat an adsorbent in the preheating section, the heating outer pipe communicates with the second medium flow channel to form a heating loop, and the temperature rising device is arranged on the heating outer pipe and used for heating the heat exchange medium in the heating loop. According to the flue gas coupling regeneration system, heat of high-temperature flue gas before cooling is used for preheating the adsorbent, a heating device does not need to be arranged, and heating energy consumption is reduced. And the cooling section directly utilizes the adsorbed low-temperature flue gas for cooling, so that the stability is better. The heat exchange medium of the heating section is not used for heating of the preheating section any more, and energy consumption can be reduced.

Description

Technical Field

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

[0002] The large amount of pollutants produced by coal-fired flue gas is one of the important factors that endanger the atmospheric environment and human health. In the relevant technology, a flue gas adsorption tower is often used to remove pollutants from the flue gas. Traditional flue gas adsorption is usually high-temperature adsorption (the flue gas temperature is about 200°C), which has the problems of large adsorbent consumption, poor adsorption effect, high nitrogen oxide content in the clean flue gas after adsorption, and inability to achieve near-zero emissions. The relevant technology proposes a flue gas low-temperature adsorption technology, which is to cool the flue gas to a low-temperature flue gas below room temperature, for example, and then remove the pollutant components in the flue gas by adsorption. 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 to conventional high-temperature flue gas adsorption, and can achieve near-zero emissions of flue gas.

[0003] The low-temperature flue gas adsorption system in the related technology adopts a low-temperature adsorption tower to adsorb and purify the flue gas, and adopts a regeneration tower to heat and regenerate the adsorbent that is saturated with adsorption. The traditional regeneration method of the regeneration tower adopts one-stage heating, that is, the adsorbent entering the regeneration tower is directly heated to the regeneration temperature, and then the desorbed and regenerated adsorbent is output from the regeneration tower. However, the one-stage heating regeneration requires a large amount of heat to be provided at one time, the load of the heater is large, the energy consumption and cost of the regeneration system remain high, and the temperature of the adsorbent after heating and regeneration is high. It is directly sent to the low-temperature adsorption tower to contact with the low-temperature flue gas, which greatly affects the adsorption efficiency of the low-temperature adsorption module and affects the further development of 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 flue gas coupled regeneration system.

[0007] The invention also provides a low-temperature flue gas adsorption system.

[0008] The flue gas coupled regeneration system of the present invention 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, wherein the preheating section has a first medium flow channel for circulating a heat exchange medium, the heating section has a second medium flow channel for circulating a heat exchange medium, and the cooling section has a third medium flow channel for circulating a heat exchange medium; a heat exchanger, wherein the hot side inlet of the heat exchanger is connected to the high-temperature flue gas outlet of the economizer, and the cold side of the heat exchanger is connected to the first medium flow channel, and the high-temperature flue gas input from the economizer to the heat exchanger exchanges heat with the heat exchange medium on the cold side of the heat exchanger to heat the heat exchange medium and then input the first medium flow channel to preheat the adsorbent in the preheating section; a heating device and a heating outer tube, wherein the heating outer tube is connected to the second medium flow channel to form a heating circuit, and the heating device is arranged on the heating outer tube to heat the heat exchange medium in the heating circuit.

[0009] Optionally, the third medium flow channel is used to pass purified low-temperature flue gas, and the low-temperature flue gas is used to cool the adsorbent in the cooling section. The temperature of the low-temperature flue gas is below room temperature.

[0010] Optionally, the regeneration system further includes a mixing tube, the outlet end of which is connected to the inlet of the first medium flow channel, and the mixing tube is used to input a temperature-adjusting medium, and the temperature-adjusting medium is mixed with the heat exchange medium at the outlet of the cold side of the heat exchanger to adjust the temperature of the heat exchange medium input to the first medium flow channel. For example, in some cases, the mixing tube is used to input a temperature-adjusting medium with a lower temperature to adjust the preheating temperature of the preheating section to avoid the preheating temperature being too high. This causes the adsorbent to release a large amount of water vapor during the preheating process of the adsorbent in the preheating section, which is not conducive to the timely extraction of water vapor, and the water vapor contacts and agglomerates with the adsorbent, causing the blockage of the feed pipe.

[0011] Optionally, at least one of the first medium flow channel, the second medium flow channel, and the third medium flow channel is a serpentine flow channel. The residence time of the heat exchange medium in the regeneration tower is prolonged to achieve a better heat exchange effect and improve energy utilization efficiency.

[0012] Optionally, 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 for the adsorbent to fall.

[0013] Optionally, 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 material distribution cavity is provided with a first suction port located above the material distribution layer to timely extract the regeneration gas generated in the preheating section and the material distribution layer. The first transition cavity is provided with a second suction port, and / or the second transition cavity is provided with a third suction port, which is used to timely extract the regeneration gas to prevent the water vapor in the regeneration gas from causing the material to agglomerate.

[0014] Optionally, in the preheating section, the heat exchange medium preheats the adsorbent to 80 degrees Celsius-110 degrees Celsius; in the heating section, the heat exchange medium heats the adsorbent to 250 degrees Celsius-350 degrees Celsius; in the cooling section, the heat exchange medium cools the adsorbent to 50 degrees Celsius-100 degrees Celsius.

[0015] The low-temperature flue gas adsorption system provided by the present invention comprises: a low-temperature adsorption module, wherein the low-temperature adsorption module has a flue gas inlet and a flue gas outlet, and low-temperature flue gas below room temperature enters the low-temperature adsorption module from the flue gas inlet, contacts with the adsorbent for adsorption, and becomes clean flue gas and is discharged from the flue gas outlet; a regeneration system, wherein the regeneration system is used to regenerate the adsorption saturated adsorbent discharged from the low-temperature adsorption module and return the regenerated adsorbent to the low-temperature adsorption module.

[0016] Optionally, the flue gas outlet is connected to the inlet of the third medium flow channel. The clean flue gas is input into the third medium flow channel as the low-temperature medium of the cooling section to cool the adsorbent. In other words, the cooling capacity required for cooling the adsorbent can come from the low-temperature clean flue gas discharged from the flue gas outlet of the low-temperature adsorption module, thereby further recycling the cooling capacity in the flue gas and avoiding the loss of cooling capacity.

[0017] Optionally, the low-temperature flue gas adsorption system also includes a cold recovery device for recovering cold in the flue gas, and the flue gas outlet is also connected to the cold recovery device so that a part of the clean flue gas discharged from the smoke gas outlet enters the third medium flow channel, and the other part enters the cold recovery device, and the outlet of the cold recovery device and the outlet of the third medium flow channel are both connected to the flue gas emission equipment.

[0018] The flue gas coupled regeneration system 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 low-temperature adsorption module for adsorption, which reduces the contact temperature between the adsorbent and the flue gas in the low-temperature adsorption module, and helps to improve the adsorption efficiency of the low-temperature adsorption module.

[0019] In addition, the heat of high-temperature flue gas before cooling is used to preheat the adsorbent, and there is no need to set up a heating device, which reduces heating energy consumption. The flue gas temperature can be reduced after heat exchange with the preheating section, reducing the heat load during subsequent flue gas cooling, which can reduce the selection of refrigeration equipment, reduce investment, and reduce energy consumption. The heat exchange medium discharged from the preheating outlet of the preheating section is self-circulated and no longer input into the boiler for reuse, which reduces the number and length of pipelines, reduces the equipment construction cost and equipment complexity. In addition, the heat exchange medium in the heating section is self-circulated and is no longer used for heating the preheating section, which can reduce energy consumption. 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. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 It is a structural schematic diagram of a flue gas coupling regeneration system provided in an embodiment of the present invention.

[0021] Reference numerals:

[0022] Regeneration system 100, regeneration tower 110, preheating section 111, first medium flow channel 1111, heating section 112, second medium flow channel 1121, cooling section 113, third medium flow channel 1131, 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, third suction port 1193, heat exchanger 120, hot side inlet 121, preheating outer tube 122, temperature raising device 130, heating outer tube 140, mixing tube 150, partition 160, low temperature adsorption module 200, cold recovery module 300. 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 Description The embodiment of the present invention provides a flue gas coupled regeneration system 100. The regeneration system 100 includes a regeneration tower 110, a heat exchanger 120, a temperature increasing device 130 and a heating outer pipe 140.

[0025] The regeneration tower 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 to achieve regeneration. The preheating section 111 is used for preheating the adsorbent, and the heating section 112 is used to heat the preheated adsorbent to regenerate and desorb 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. A first medium flow channel 1111 for circulating a heat exchange medium is defined in the preheating section 111, a second medium flow channel 1121 for circulating a heat exchange medium is defined in the heating section 121, and a third medium flow channel 1131 for circulating a heat exchange medium is defined in the cooling section 113.

[0026] The heat exchanger 120 has a hot side and a cold side, a high-temperature heat exchange medium flows through the hot side, and a low-temperature heat exchange medium flows through the cold side. The hot side inlet 121 is connected to the high-temperature flue gas outlet of the economizer, and the cold side of the heat exchanger 120 is connected to the first medium flow channel 1111. The high-temperature flue gas input from the economizer to the heat exchanger 120 exchanges heat with the heat exchange medium on the cold side of the heat exchanger 120 to heat the heat exchange medium and then input it into the first medium flow channel 1111 to preheat the adsorbent in the preheating section 111.

[0027] The heating outer tube 130 is connected to the second medium flow channel 1121 to form a heating circuit. The temperature increasing device 130 is arranged on the heating outer tube 140 and is used to heat the heat exchange medium in the heating circuit to heat the adsorbent in the heating section 112 to complete the desorption of the adsorbent.

[0028] The adsorbent discharged from the low-temperature adsorption module 200 after adsorption saturation falls from the top of the regeneration tower 110, passes through the preheating section 111, the heating section 112, and the cooling section 113 in sequence to complete desorption regeneration and cooling, and is discharged from the bottom of the regeneration tower 110 and returns to the low-temperature adsorption module for recycling.

[0029] The flue gas coupling regeneration system 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 low-temperature adsorption module for adsorption, which reduces the contact temperature between the adsorbent and the flue gas in the low-temperature adsorption module, and helps to improve the adsorption efficiency of the low-temperature adsorption module.

[0030] In addition, the heat of high-temperature flue gas before cooling is used to preheat the adsorbent, and there is no need to set up a heating device, which reduces heating energy consumption. The flue gas temperature can be reduced after heat exchange with the preheating section, reducing the heat load during subsequent flue gas cooling, which can reduce the selection of refrigeration equipment, reduce investment, and reduce energy consumption. The heat exchange medium discharged from the preheating outlet of the preheating section is self-circulated and no longer input into the boiler for reuse, which reduces the number and length of pipelines, reduces the equipment construction cost and equipment complexity. In addition, the heat exchange medium in the heating section is self-circulated and is no longer used for heating the preheating section, which can reduce energy consumption. 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.

[0031] The flue gas coupling regeneration system provided by the present invention can be applied to the heating regeneration of activated carbon after low-temperature adsorption of activated carbon.

[0032] In some embodiments, the third medium flow channel 1131 is used to pass purified low-temperature flue gas, and the low-temperature flue gas is used to cool the adsorbent in the cooling section 113. The temperature of the low-temperature flue gas is below room temperature.

[0033] In some preferred embodiments, the temperature of the low-temperature flue gas is below zero, for example, -80°C to -5°C.

[0034] More preferably, the temperature of the low-temperature flue gas is -20°C to -5°C.

[0035] Optionally, the heat exchange medium flowing through the preheating section 111 and the heating section 112 may be gas or liquid.

[0036] Preferably, in order to reduce operating costs, the heat exchange medium circulating in the preheating section 111 and the heating section 112 is air.

[0037] In some embodiments, Figure 1 As shown, the flue gas coupled regeneration system also includes a mixing tube 150, the outlet end of the mixing tube 150 is connected to the inlet of the first medium flow channel 1111, and the mixing tube 150 is used to input a temperature regulating medium. The temperature regulating medium is mixed with the heat exchange medium at the cold side outlet of the heat exchanger 120 to adjust the temperature of the heat exchange medium input to the first medium flow channel 1111, and the temperature of the heat exchange medium input to the first medium flow channel 1111 is controlled within a preset range.

[0038] For example, in some cases, the mixing tube 150 is used to input a temperature-adjusting medium with a relatively low temperature to adjust the preheating temperature of the preheating section 111 to avoid the preheating temperature being too high, which causes the adsorbent to release a large amount of water vapor during the preheating process of the adsorbent in the preheating section 111, making it difficult for the water vapor to be drawn away in time, and the water vapor agglomerates with the adsorbent, causing the blockage of the feed pipe.

[0039] In some cases, the mixing tube 150 is used to input a temperature-adjusting medium with a relatively high temperature to adjust the preheating temperature of the preheating section 111 to avoid the preheating temperature being too low.

[0040] Optionally, the preheating temperature in the preheating section 111 is controlled to be less than 150 degrees Celsius.

[0041] Preferably, the preheating temperature in the preheating section 111 is controlled to be less than 110 degrees Celsius.

[0042] As an example, Figure 1 As shown, the flue gas coupled regeneration system 100 includes a preheating outer tube 122, the cold side of the heat exchanger 120 is connected to the first medium flow channel 1111 through the preheating outer tube 122 to form a preheating loop, the outlet end of the mixing tube 150 is connected to the preheating outer tube 122, and the heat exchange medium in the preheating loop is air. The cooling medium input into the mixing tube 150 is air.

[0043] In some preferred embodiments, 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 1111, the second medium flow channel 1121, and the third medium flow channel 1131 is a serpentine flow channel.

[0044] As an example, in Figure 1In 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 1111, a serpentine second medium flow channel 1121 and a serpentine third medium flow channel 1131 in the preheating section 111, the heating section 112 and the cooling section 113, respectively.

[0045] 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 .

[0046] like Figure 1 As 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 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.

[0047] In the preheating section 111, a first medium flow channel 1111 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 1121 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 1131 is defined between the outer side of the third feed pipe 1173 and the inner wall surface of the regeneration tower 110.

[0048] Furthermore, if Figure 1As shown, a material distribution cavity for forming a material distribution layer 1181 is provided above the first material discharge pipe 1171. A first transition cavity for forming a first material distribution layer 1182 is provided between the preheating section 111 and the heating section 112, and a second transition cavity for forming a second material distribution layer 1183 is provided between the heating section 112 and the cooling section 113. The material distribution layer 1181 is formed by the adsorbent entering the regeneration tower 110 from the regeneration inlet 115 and piled up on the top of the first material discharge pipe 1171. The adsorbent in the material distribution layer 1181 gradually falls into the first material discharge pipe 1171. A first material distribution layer 1182 is formed between the preheating section 111 and the heating section 112, that is, a first material distribution layer 1182 is formed between the first material distribution layer and the second material distribution layer. A second material distribution layer 1183 is formed between the heating section 112 and the cooling section 113, that is, a second material distribution layer 1183 is formed between the second material distribution layer and the third material distribution layer. The second stacking layer 1183 is also called the degassing section. The adsorbent is mainly degassed and regenerated in this layer.

[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 1 As shown, the cloth chamber is provided with a first suction port 1191 located above the cloth layer 1181, which is used to timely extract the regeneration gas generated in the preheating section 111 and the cloth layer 1181.

[0051] In some embodiments, Figure 1 As 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] Furthermore, in some embodiments, Figure 1 As shown, the second transition chamber is provided with a third suction port 1193 for timely extracting the regeneration gas to prevent the water vapor in the regeneration gas from causing the material to agglomerate.

[0053] In some embodiments, the adsorbent is preliminarily heated to 80 degrees Celsius-110 degrees Celsius in the preheating section 111; the adsorbent is heated to 250 degrees Celsius-350 degrees Celsius in the heating section 112 to desorb and regenerate the adsorbent; and the adsorbent is cooled to 50 degrees Celsius-100 degrees Celsius in the cooling section 113.

[0054] In some specific embodiments, the adsorbent is preliminarily heated to 100 degrees Celsius in the preheating section 111; the adsorbent is heated to 300 degrees Celsius in the heating section 112 to desorb and regenerate the adsorbent; and the adsorbent is cooled to 80 degrees Celsius in the cooling section 113.

[0055] Another embodiment of the present invention further provides a low-temperature flue gas adsorption system, which includes a low-temperature adsorption module 200 and a regeneration system 100, wherein the regeneration system 100 is the regeneration system 100 in any of the above embodiments.

[0056] The low-temperature adsorption module 200 has a flue gas inlet and a flue gas outlet. Low-temperature flue gas below room temperature enters the low-temperature adsorption module 200 from the flue gas inlet, contacts with the adsorbent for adsorption, and becomes clean flue gas and is discharged from the flue gas outlet. The regeneration system 100 is used to regenerate the adsorbent saturated with adsorption discharged from the low-temperature adsorption module and return the regenerated adsorbent to the low-temperature adsorption module. The low-temperature adsorption module 200 also has a feed inlet and a discharge port (not shown in the figure). The regeneration outlet 116 of the regeneration system 100 is connected to the feed inlet of the low-temperature adsorption module 200, and the discharge port of the low-temperature adsorption module is connected to the regeneration inlet 115 of the regeneration system 100, so that the adsorbent saturated with adsorption is sent into the regeneration system 100 for regeneration.

[0057] Preferably, the temperature of the low-temperature flue gas is below zero.

[0058] More preferably, the temperature of the low-temperature flue gas is minus 20 degrees Celsius to minus 15 degrees Celsius.

[0059] The following briefly describes the regeneration process of the adsorbent regeneration using the regeneration system 100, which includes:

[0060] Preheating step: In the preheating section 111, the adsorbent entering the regeneration system 100 is preheated to 80 degrees Celsius to 110 degrees Celsius;

[0061] Heating step: In the heating section 112, the preheated adsorbent is heated to 250 degrees Celsius to 350 degrees Celsius to desorb and regenerate the adsorbent;

[0062] Cooling step: In the cooling section 113, the regenerated adsorbent is cooled to 50 degrees Celsius to 100 degrees Celsius. The cooled adsorbent can then be input into the low-temperature adsorption module 100 for adsorption.

[0063] Adding a cooling step in the regeneration process to pre-cool the adsorbent temperature to below 100 degrees Celsius can ensure that the temperature of the low-temperature adsorbent after heat exchange is sufficiently low to further improve the adsorption efficiency. Since the adsorbent can be cooled by heat exchange with the low-temperature clean flue gas after entering the low-temperature adsorption module 200, the cooling load in the cooling step is low, which helps to reduce the structural complexity of the regeneration system 100 and the regeneration cost.

[0064] Furthermore, the flue gas outlet of the low-temperature adsorption module 200 is connected to the third medium flow channel 1131 of the cooling section 113, and the clean flue gas is input into the third medium flow channel 1131 as the low-temperature medium of the cooling section 113 to cool the adsorbent. In other words, the cold energy required for cooling the adsorbent in the above cooling step can come from the low-temperature clean flue gas discharged from the flue gas outlet of the low-temperature adsorption module 200, thereby further recycling the cold energy in the flue gas and avoiding the loss of cold energy.

[0065] In a specific embodiment, the regeneration process comprises:

[0066] Preheating step: In the preheating section 111, the adsorbent is preheated to 100 degrees Celsius;

[0067] Heating step: in the heating section 112, the preheated adsorbent is heated to 300 degrees Celsius to desorb and regenerate the adsorbent;

[0068] Cooling step: In the cooling section 113, the low-temperature clean flue gas discharged from the low-temperature adsorption module from the flue gas outlet cools the regenerated adsorbent to 80 degrees Celsius.

[0069] In some embodiments, Figure 1 As shown, the low-temperature flue gas adsorption system also includes a cold energy recovery device 300 for recovering cold energy in the flue gas. The flue gas outlet of the low-temperature adsorption module 200 is also connected to the cold energy recovery device 300 so that a part of the clean flue gas discharged from the flue gas outlet enters the third medium flow channel 1131, and the other part enters the cold energy recovery device 300. The outlet of the cold energy recovery device 300 and the outlet of the third medium flow channel 1131 are both connected to the flue gas emission equipment.

[0070] 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.

[0071] 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.

[0072] 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.

[0073] 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.

[0074] 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.

[0075] 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 flue gas coupling regeneration system, characterized in that: include: A regeneration tower, the regeneration tower 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 having a first medium flow channel for circulating a heat exchange medium, the heating section having a second medium flow channel for circulating a heat exchange medium, and the cooling section having a third medium flow channel for circulating a heat exchange medium; A heat exchanger, wherein the hot side inlet of the heat exchanger is connected to the high-temperature flue gas outlet of the economizer, and the cold side of the heat exchanger is connected to the first medium flow channel, and the high-temperature flue gas input from the economizer to the heat exchanger exchanges heat with the heat exchange medium on the cold side of the heat exchanger to heat the heat exchange medium and then input it into the first medium flow channel to preheat the adsorbent in the preheating section; A temperature increasing device and a heating outer tube, wherein the heating outer tube is connected with the second medium flow channel to form a heating circuit, and the temperature increasing device is arranged on the heating outer tube and is used to heat the heat exchange medium in the heating circuit.

2. The flue gas coupling regeneration system according to claim 1, characterized in that: The third medium flow channel is used to pass the purified low-temperature flue gas, and the low-temperature flue gas is used to cool the adsorbent in the cooling section. The temperature of the low-temperature flue gas is below room temperature.

3. The flue gas coupling regeneration system according to claim 1, characterized in that: It also includes a mixing tube, the outlet end of which is connected to the inlet of the first medium flow channel. The mixing tube is used to input a temperature regulating medium, and the temperature regulating medium is mixed with the heat exchange medium at the cold side outlet of the heat exchanger to adjust the temperature of the heat exchange medium input into the first medium flow channel.

4. The flue gas coupling regeneration system according to claim 1, characterized in that: At least one of the first medium flow channel, the second medium flow channel, and the third medium flow channel is a serpentine flow channel.

5. The flue gas coupling regeneration system 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 for the adsorbent to fall.

6. The flue gas coupling regeneration system according to claim 5, characterized in that: 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 accumulation layer is provided between the preheating section and the heating section, a second transition cavity for forming a second material accumulation layer is provided between the heating section and the cooling section, and the material distribution cavity is provided with a first suction port located above the material distribution layer; The first transition chamber is provided with a second suction port, and / or the second transition chamber is provided with a third suction port.

7. The flue gas coupled regeneration system according to any one of claims 1 to 6, characterized in that: In the preheating section, the heat exchange medium preheats the adsorbent to 80 degrees Celsius to 110 degrees Celsius; In the heating section, the heat exchange medium heats the adsorbent to 250 degrees Celsius to 350 degrees Celsius; In the cooling section, the heat exchange medium cools the adsorbent to 50 degrees Celsius to 100 degrees Celsius.

8. A low-temperature flue gas adsorption system, characterized in that: include: A low-temperature adsorption module, wherein the low-temperature adsorption module has a flue gas inlet and a flue gas outlet. Low-temperature flue gas below room temperature enters the low-temperature adsorption module from the flue gas inlet, contacts with the adsorbent for adsorption, and becomes clean flue gas and is discharged from the flue gas outlet; A regeneration system, wherein the regeneration system is a regeneration system according to any one of claims 1 to 7, and the regeneration system is used to regenerate the adsorption saturated adsorbent discharged from the low-temperature adsorption module and return the regenerated adsorbent to the low-temperature adsorption module.

9. The low-temperature flue gas adsorption system according to claim 8, characterized in that: The smoke outlet is communicated with the inlet of the third medium flow channel.

10. The low-temperature flue gas adsorption system according to claim 9, characterized in that: It also includes a cold recovery device for recovering cold in the flue gas. The flue gas outlet is also connected to the cold recovery device so that a part of the clean flue gas discharged from the smoke gas outlet enters the third medium flow channel, and the other part enters the cold recovery device. The outlet of the cold recovery device and the outlet of the third medium flow channel are both connected to the flue gas emission device.

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