Carbon capture system and carbon capture method

Abstract

The invention relates to the technical field of carbon dioxide capture, and provides a carbon capture system and a carbon capture method.The carbon capture system comprises a denitration and desulfurization device, a compression device, a refrigeration device and a cold rectification device, and the inlet side of the denitration and desulfurization device is used for introducing carbon-containing waste gas; the denitration and desulfurization device, the compression device and the cold rectification device are sequentially connected through a pipeline, and the pipeline between the compression device and the cold rectification device is thermally conducted with the refrigeration end of the refrigeration device; the cold rectification device comprises a cold rectification tower, and at least one of the inlet side and the outlet side of the cold rectification tower is in thermal conduction with the refrigeration end of the refrigeration device. The problem that the energy utilization rate is low in carbon dioxide capture, utilization and storage can be solved.

Description

Technical Field

[0001] The present application relates to the technical field of carbon dioxide capture, and in particular to a carbon capture system and a carbon capture method. Background Art

[0002] Carbon dioxide capture, utilization and storage refers to the process of separating carbon dioxide from industrial processes, energy utilization or the atmosphere, and utilizing it or directly injecting it into the formation to achieve permanent reduction of carbon dioxide emissions.

[0003] In the related technologies, carbon dioxide capture, utilization and storage have the problem of low energy utilization rate. Summary of the invention

[0004] The present application provides a carbon capture system and a carbon capture method for solving the problem of low energy utilization rate in carbon dioxide capture, utilization and storage.

[0005] In order to achieve the above objectives, this application adopts the following technical solutions:

[0006] In a first aspect, the present application provides a carbon capture system, comprising:

[0007] Denitration and desulfurization device, compression device, refrigeration device and cold distillation device, the inlet side of the denitration and desulfurization device is used to pass carbon-containing waste gas;

[0008] The denitration and desulfurization device, the compression device and the cold distillation device are connected in sequence through pipelines, and the pipeline between the compression device and the cold distillation device is thermally connected to the refrigeration end of the refrigeration device;

[0009] The cold distillation device comprises a cold distillation tower, at least one of the inlet side and the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device.

[0010] In a feasible embodiment, the compression device has an inlet and an outlet, the inlet of the compression device is connected to the outlet of the denitration and desulfurization device through a pipeline, and the outlet of the compression device is connected to the inlet side of the cold distillation tower through another pipeline.

[0011] In a feasible embodiment, the cold distillation device further includes a first pipeline assembly, a second pipeline assembly, a third pipeline assembly, a fourth pipeline assembly and a tower top condenser, and the tower top condenser is arranged at the outlet side of the cold distillation tower;

[0012] The inlet side of the cold distillation tower is connected to the outlet of the compression device through the first pipeline assembly;

[0013] The bottom outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device through the second pipeline assembly;

[0014] The bottom outlet side of the cold distillation tower is connected to the top condenser through a third pipeline assembly;

[0015] The outlet side of the tower top condenser is communicated with at least the compression device through a fourth pipeline assembly.

[0016] In a feasible embodiment, a first throttle valve is provided on the third pipeline assembly, and the first throttle valve is used to communicate with the bottom outlet side of the cold distillation tower and the top condenser through the third pipeline assembly respectively;

[0017] The first pipeline assembly includes a first sub-pipeline and a second sub-pipeline, and the fourth pipeline assembly includes a third sub-pipeline and a fourth sub-pipeline; the first sub-pipeline is provided with a residual cooling heat exchanger and is thermally connected to the third sub-pipeline, the second sub-pipeline is provided with a refrigeration system heat exchanger and is thermally connected to the second pipeline assembly, and the fourth sub-pipeline is connected to the outlet of the compression device.

[0018] In a feasible implementation, the refrigeration device includes a refrigeration distillation tower, a condenser, a reboiler, an ammonia cooler, a liquid ammonia buffer tank, a concentrated ammonia water preheater, an ammonia absorption tank, and a second throttle valve;

[0019] The refrigeration distillation tower, the ammonia cooler, the liquid ammonia buffer tank, the second throttle valve and the concentrated ammonia water preheater are connected in sequence through pipelines;

[0020] The refrigeration distillation tower is connected to the condenser via a first connecting pipe;

[0021] The reboiler is connected to the refrigeration distillation tower via a second connecting pipe;

[0022] The concentrated ammonia water preheater is connected to the refrigeration distillation tower via a third connecting pipe;

[0023] The liquid ammonia buffer tank and the ammonia gas absorption tank are connected by a pipeline to form a refrigeration end of the refrigeration device, and the throttle valve is located at the refrigeration end;

[0024] A portion of the pipeline located at the refrigeration end is thermally connected to the second sub-pipeline through a refrigeration system heat exchanger;

[0025] And / or, another part of the pipeline at the refrigeration end is thermally connected to the second pipeline assembly through the product heat exchanger.

[0026] In a feasible embodiment, the denitration and desulfurization device includes a denitration component and a desulfurization component, the inlet end of the denitration component is used for introducing carbon-containing exhaust gas, the outlet end of the denitration component is connected to the inlet end of the desulfurization component through a pipeline, and the outlet end of the desulfurization component is connected to the inlet of the compression device through another pipeline;

[0027] Alternatively, the inlet end of the desulfurization component is used for introducing carbon-containing exhaust gas, the outlet end of the desulfurization component is connected to the inlet end of the denitrification component through a pipeline, and the outlet end of the denitrification component is connected to the inlet of the compression device through another pipeline.

[0028] In a feasible embodiment, the desulfurization component includes a venturi chiller, the inlet of the venturi chiller forms the inlet side of the denitration and desulfurization device, and the outlet of the venturi chiller is connected to the denitration component;

[0029] And / or, the denitration component includes an SCR reactor and a waste heat boiler, the inlet of the waste heat boiler forms the inlet side of the denitration and desulfurization device, the outlet of the waste heat boiler is connected to the inlet of the SCR reactor, and the outlet of the SCR reactor is connected to the desulfurization component.

[0030] In a feasible embodiment, the compression device is a three-stage compression assembly, one end of the three-stage compression assembly is connected to the denitration and desulfurization device, and the other end of the three-stage compression assembly is connected to the cold distillation tower.

[0031] In a second aspect, the present application provides a carbon capture method, which is applied to a carbon capture system. The carbon capture method comprises:

[0032] Desulfurization and denitration treatment, passing the carbon-containing waste gas into a denitration and desulfurization device to remove at least part of the sulfur dioxide gas and a small part of nitrogen oxides in the carbon-containing waste gas, and obtain a first gas;

[0033] Compression treatment, passing the first gas through a three-stage compression assembly to remove water vapor in the first gas and obtain a second gas;

[0034] Cooling treatment, using a refrigeration device to cool the second gas so that at least part of the second gas is liquefied to form a gas-liquid mixture;

[0035] Cold distillation treatment, passing the gas-liquid mixture into a cold distillation tower to separate the gas and liquid in the gas-liquid mixture to obtain a low-temperature and high-pressure first liquid and a low-temperature third gas;

[0036] Heat exchange treatment is performed to conduct heat between the low-temperature and high-pressure first liquid and the refrigeration device to obtain the first liquid at room temperature and high pressure, and / or, heat conduction is performed between the low-temperature third gas and the refrigeration device to obtain the third gas at room temperature.

[0037] In a feasible embodiment, the desulfurization and denitrification treatment includes:

[0038] Pretreatment: The carbon-containing waste gas is passed into the waste heat boiler to cool the carbon-containing waste gas to 100℃-200℃;

[0039] Denitration: passing the carbon-containing waste gas at 100°C-200°C into the denitration component to remove at least part of the nitrogen oxides in the carbon-containing waste gas and obtain a first pretreated gas;

[0040] Desulfurization: passing the first pretreated gas into a desulfurization component to remove at least part of sulfur dioxide gas in the first pretreated gas to obtain a first gas;

[0041] Or, desulfurization: passing the carbon-containing waste gas into a desulfurization component to remove at least part of sulfur dioxide gas in the carbon-containing waste gas and obtain a second pretreated gas;

[0042] Denitration: The second pretreated gas is introduced into the denitration component to remove at least part of nitrogen oxides in the second pretreated gas to obtain the first gas.

[0043] The present application provides a carbon capture system and a carbon capture method, which include: a denitration and desulfurization device, a compression device, a refrigeration device and a cold distillation device, wherein the inlet side of the denitration and desulfurization device is used to introduce carbon-containing exhaust gas; the denitration and desulfurization device, the compression device and the cold distillation device are connected in sequence through pipelines, and the pipeline between the compression device and the cold distillation device is thermally connected to the refrigeration end of the refrigeration device; the cold distillation device includes a cold distillation tower, and at least one of the inlet side and the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device.

[0044] In the carbon capture system of this structure, the denitrification and desulfurization device is used to remove nitrogen oxides and sulfur dioxide in the carbon-containing gas, the compression device is used to remove water vapor in the carbon-containing gas, the refrigeration device is used to cool the carbon-containing gas so that part of the gas in the carbon-containing gas can be liquefied, and the cold distillation device is used to perform cold distillation on the liquefied part of the gas and the non-liquefied gas so that the carbon dioxide in the liquefied part of the gas and the non-liquefied gas can be liquefied into liquid carbon dioxide, thereby separating the liquid carbon dioxide from the nitrogen.

[0045] It can be understood that the pipeline between the compression device and the cold distillation device is thermally connected to the refrigeration end of the refrigeration device, so that the pipeline between the compression device and the cold distillation device can exchange heat with the refrigeration end of the refrigeration device to reduce the surface temperature of the pipeline between the compression device and the cold distillation device, thereby improving the utilization rate of the cold capacity of the refrigeration device, improving the utilization rate of the cold capacity between the compression device and the cold distillation device, and improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0046] It can be understood that at least one of the inlet side and the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device. When the inlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device, the carbon-containing gas entering the cold distillation tower can be pre-cooled to reduce the cold consumption of the cold distillation tower, and the cold utilization rate of the refrigeration device can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage. When the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device, the gas or liquid derived from the outlet side of the cold distillation tower can cool the refrigeration device to improve the cold utilization rate of the gas or liquid derived from the outlet side of the cold distillation tower, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0047] Therefore, the carbon capture system provided in the embodiments of the present application can solve the problem of low energy utilization rate in carbon dioxide capture, utilization and storage. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0049] Figure 1 A schematic diagram of the process structure of the carbon capture method provided in the embodiment of the present application;

[0050] Figure 2 A schematic diagram of the connection structure of the cold distillation device provided in the embodiment of the present application;

[0051] Figure 3 A schematic diagram of the connection structure of the compression device provided in an embodiment of the present application;

[0052] Figure 4 A schematic diagram of the connection structure of a refrigeration device provided in an embodiment of the present application.

[0053] Description of reference numerals:

[0054] 100-Denitration and desulfurization device;

[0055] 101- denitrification component;

[0056] 1011-SCR reactor;

[0057] 1012-waste heat boiler;

[0058] 102- desulfurization component;

[0059] 1021-Venturi chiller;

[0060] 200-compression device;

[0061] 300- Refrigeration equipment;

[0062] 301-refrigeration distillation tower;

[0063] 302- condenser;

[0064] 303- reboiler;

[0065] 304- ammonia cooler;

[0066] 305-liquid ammonia buffer tank;

[0067] 306- concentrated ammonia water preheater;

[0068] 307-Ammonia absorption tank;

[0069] 308 - second throttle valve;

[0070] 309- Refrigeration system heat exchanger;

[0071] 3010-Product heat exchanger;

[0072] 400-cold distillation unit;

[0073] 401-cold distillation tower;

[0074] 402-first pipeline assembly;

[0075] 4021-first sub-pipeline;

[0076] 4022-second sub-pipeline;

[0077] 403-second pipeline assembly;

[0078] 404-third pipeline assembly;

[0079] 4041-first throttle valve;

[0080] 405- fourth pipeline assembly;

[0081] 4051-third sub-pipeline;

[0082] 4052-the fourth sub-pipeline;

[0083] 406-tower top condenser;

[0084] 407- waste cooling heat exchanger;

[0085] 408-Line pump. DETAILED DESCRIPTION

[0086] In order to make the purpose, technical scheme and advantages of the embodiments of the present application clearer, the technical scheme in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, rather than all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application. In the absence of conflict, the following embodiments and features in the embodiments can be combined with each other.

[0087] In the prior art, carbon-containing waste gas is a gas enriched with high concentrations of carbon dioxide in industrial flue gas by replacing air with a mixture of high-concentration oxygen and flue gas.

[0088] It should be noted that carbon-containing waste gas contains a certain amount of nitrogen oxides and sulfur dioxide. In the industrial process of carbon dioxide capture, utilization and storage, it is necessary to remove nitrogen oxides and sulfur dioxide from the carbon-containing waste gas.

[0089] In the related art, the removal of nitrogen oxides and sulfur dioxide in carbon-containing exhaust gas has a low energy utilization rate, which will lead to a low energy utilization rate of the carbon capture system.

[0090] In order to overcome the defects in the prior art, the present application provides a carbon capture system, wherein a denitration and desulfurization device is used to remove nitrogen oxides and sulfur dioxide in carbon-containing gas, a compression device is used to remove water vapor in the carbon-containing gas, a refrigeration device is used to cool the carbon-containing gas so that part of the gas in the carbon-containing gas can be liquefied, and a cold distillation device is used to perform cold distillation treatment on the liquefied part of the gas and the non-liquefied gas so that the carbon dioxide in the liquefied part of the gas and the non-liquefied gas can be liquefied into liquid carbon dioxide, thereby separating the liquid carbon dioxide from the nitrogen.

[0091] It can be understood that the pipeline between the compression device and the cold distillation device is thermally connected to the refrigeration end of the refrigeration device, so that the pipeline between the compression device and the cold distillation device can exchange heat with the refrigeration end of the refrigeration device to reduce the surface temperature of the pipeline between the compression device and the cold distillation device, thereby improving the utilization rate of the cold capacity of the refrigeration device, improving the utilization rate of the cold capacity between the compression device and the cold distillation device, and improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0092] It can be understood that at least one of the inlet side and the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device. When the inlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device, the carbon-containing gas entering the cold distillation tower can be pre-cooled to reduce the cold consumption of the cold distillation tower, and the cold utilization rate of the refrigeration device can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage. When the outlet side of the cold distillation tower is thermally connected to the refrigeration end of the refrigeration device, the gas or liquid derived from the outlet side of the cold distillation tower can cool the refrigeration device to improve the cold utilization rate of the gas or liquid derived from the outlet side of the cold distillation tower, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0093] Therefore, the carbon capture system provided in the embodiments of the present application can solve the problem of low energy utilization rate in carbon dioxide capture, utilization and storage.

[0094] The contents of the present application will be described in detail below in conjunction with the accompanying drawings so that those skilled in the art can understand the contents of the present application more clearly and in detail.

[0095] The specific structure of the carbon capture system and various possible implementation methods are described in detail below.

[0096] like Figure 1 and Figure 2 As shown, an embodiment of the present application provides a carbon capture system, comprising: a denitration and desulfurization device 100, a compression device 200, a refrigeration device 300 and a cold distillation device 400, the inlet side of the denitration and desulfurization device 100 is used to introduce carbon-containing exhaust gas; the denitration and desulfurization device 100, the compression device 200 and the cold distillation device 400 are connected in sequence through pipelines, and the pipeline between the compression device 200 and the cold distillation device 400 is thermally connected to the refrigeration end of the refrigeration device 300; the cold distillation device 400 includes a cold distillation tower 401, and at least one of the inlet side and the outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300.

[0097] It should be noted that there are various heat conduction positions for thermal conduction between the cold distillation tower 401 and the refrigeration end of the refrigeration device 300. The heat conduction positions for thermal conduction between the cold distillation tower 401 and the refrigeration end of the refrigeration device 300 are described below with examples.

[0098] In a feasible implementation, the inlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 .

[0099] It can be understood that the thermal conduction between the inlet side of the cold distillation tower 401 and the refrigeration end of the refrigeration device 300 can enable the carbon-containing gas entering the cold distillation tower 401 to be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and can improve the cold utilization rate of the refrigeration device 300, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0100] In another feasible embodiment, the outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 .

[0101] It can be understood that the outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300, and the gas or liquid discharged from the outlet side of the cold distillation tower 401 can cool the refrigeration device 300 to improve the cold capacity utilization rate of the gas or liquid discharged from the outlet side of the cold distillation tower 401, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0102] In addition, in another feasible embodiment, the inlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 , and the outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 .

[0103] It can be understood that the inlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300, so that the carbon-containing gas entering the cold distillation tower 401 can be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and the cold utilization rate of the refrigeration device 300 can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage. The outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300, and the gas or liquid derived from the outlet side of the cold distillation tower 401 can cool the refrigeration device 300 to improve the cold utilization rate of the gas or liquid derived from the outlet side of the cold distillation tower 401, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0104] It is understandable that the thermal conduction position of the cold distillation tower 401 and the refrigeration end of the refrigeration device 300 is not limited and can be selected according to actual use requirements.

[0105] The compression device 200 provided in the embodiment of the present application has an inlet and an outlet. The inlet of the compression device 200 is connected to the outlet of the denitration and desulfurization device 100 through a pipeline, and the outlet of the compression device 200 is connected to the inlet side of the cold distillation tower 401 through another pipeline.

[0106] It can be understood that the compression device 200 is used to remove water vapor from the carbon-containing gas.

[0107] like Figure 3As shown, it should be noted that the compression device 200 is a three-stage compression component, one end of the three-stage compression component is connected to the denitration and desulfurization device 100, and the other end of the three-stage compression component is connected to the cold distillation tower 401.

[0108] It can be understood that the compression device 200 is a three-stage compression component, which can improve the removal efficiency of water vapor in the carbon-containing gas to improve the yield rate of the carbon capture system.

[0109] It can be understood that the three-stage compression component includes: three compressors, three heat exchangers and three demisters. Along the direction from the denitrification and desulfurization device 100 to the cold distillation tower 401, the three compressors are: a first-stage compressor, a second-stage compressor and a third-stage compressor. Along the direction from the denitrification and desulfurization device 100 to the cold distillation tower 401, the three heat exchangers are: a first-stage heat exchanger, a second-stage heat exchanger and a third-stage heat exchanger. Along the direction from the denitrification and desulfurization device 100 to the cold distillation tower 401, the three demisters are: a first-stage demister, a second-stage demister and a third-stage demister.

[0110] It should be noted that the input end of the first-stage compressor is connected to the output end of the denitrification and desulfurization device 100, the output end of the first-stage compressor is connected to the input end of the first-stage heat exchanger, the output end of the first-stage heat exchanger is connected to the input end of the first-stage demister tank, one output end of the first-stage demister tank is connected to the input end of the second-stage compressor, the other output end of the first-stage demister tank is connected to the next process, and the other output end of the first-stage demister tank is used to export the liquid water in the first-stage demister tank to the next process or the external environment.

[0111] It should be noted that the output end of the secondary compressor is connected to the input end of the secondary heat exchanger, the output end of the secondary heat exchanger is connected to the input end of the secondary demister tank, one output end of the secondary demister tank is connected to the input end of the tertiary compressor, the other output end of the secondary demister tank is connected to the next process, and the other output end of the secondary demister tank is used to export the liquid water in the secondary demister tank to the next process or the external environment.

[0112] It should be noted that the output end of the three-stage compressor is connected to the input end of the three-stage heat exchanger, the output end of the three-stage heat exchanger is connected to the input end of the three-stage demister tank, one output end of the three-stage demister tank is connected to the inlet side of the cold distillation tower 401, the other output end of the three-stage demister tank is connected to the next process, and the other output end of the three-stage demister tank is used to export the liquid water in the three-stage demister tank to the next process or the external environment.

[0113] It should be noted that the carbon-containing exhaust gas treated by the denitrification and desulfurization device 100 enters the three-stage compression assembly at normal temperature and pressure, and the pressure is increased to 2.2-4.0 bar by the first-stage compressor, and the temperature of the compressed fluid rises to 150-200°C, and then the temperature is reduced to 33-40°C by the first-stage heat exchanger, and then enters the first-stage demister to remove the condensate. Subsequently, the fluid reaches 6.8-10.2 bar through the second-stage compressor, and is heated to 140-190°C again, cooled to 28-35°C by the second-stage heat exchanger, and the condensate is removed again by the second-stage demister. Finally, the fluid is compressed to 22-28 bar by the third-stage compressor, and the compressed temperature is raised to 120-170°C again, cooled to 28-35°C by the third-stage heat exchanger, and the condensate is removed by the third-stage demister.

[0114] The condensate may be water, or a compound or solution composed of water and some substances soluble in water. There is no limitation here and they are all referred to as water.

[0115] It should be noted that the three-stage compression assembly compresses the fluid with an initial pressure of 1 bar to 22-28 bar, and removes 99.0-99.6% of the water therein.

[0116] The cold distillation device 400 provided in the embodiment of the present application also includes a first pipeline assembly 402, a second pipeline assembly 403, a third pipeline assembly 404, a fourth pipeline assembly 405 and a top condenser 406, and the top condenser 406 is arranged on the outlet side of the cold distillation tower 401; the inlet side of the cold distillation tower 401 is connected to the outlet of the compression device 200 through the first pipeline assembly 402; the bottom outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 through the second pipeline assembly 403; the bottom outlet side of the cold distillation tower 401 is connected to the top condenser 406 through the third pipeline assembly 404; the outlet side of the top condenser 406 is connected to at least the compression device 200 through the fourth pipeline assembly 405.

[0117] It can be understood that the top condenser 406 is used to condense the fluid entering the cold distillation tower 401, so that the carbon dioxide in the fluid in the cold distillation tower 401 can be liquefied into liquid carbon dioxide, thereby realizing the separation between the fluid and the liquid carbon dioxide in the cold distillation tower 401. The inlet side of the cold distillation tower 401 is connected to the outlet of the compression device 200 through the first pipeline assembly 402, so that the fluid in the compression device 200 can enter the interior of the cold distillation tower 401 after passing through the first pipeline assembly 402. The bottom outlet side of the cold distillation tower 401 is thermally connected to the refrigeration end of the refrigeration device 300 through the second pipeline assembly 403, and the low-temperature and high-pressure liquid carbon dioxide can be led to the refrigeration end of the refrigeration device 300, so that the low-temperature and high-pressure liquid carbon dioxide and the refrigeration end of the refrigeration device 300 generate heat exchange, so as to reduce the surface temperature of the refrigeration device 300, and the low-temperature and high-pressure liquid carbon dioxide can be heated to liquid carbon dioxide at room temperature and high pressure, so as to improve the cold capacity utilization rate of the low-temperature liquid carbon dioxide. The bottom outlet side of the cold distillation tower 401 is connected to the top condenser 406 through the third pipeline assembly 404, so that the fluid at the bottom outlet side of the cold distillation tower 401 can enter the top condenser 406 after passing through the third pipeline assembly 404, so that the carbon dioxide in the fluid in the cold distillation tower 401 can be liquefied into liquid carbon dioxide. The outlet side of the top condenser 406 is at least connected to the compression device 200 through the fourth pipeline assembly 405, and the fluid derived from the outlet side of the top condenser 406 can be recycled to improve the yield of liquid carbon dioxide in the carbon capture system.

[0118] It should be noted that a pipeline pump 408 is provided on the second pipeline assembly 403 , and the pipeline pump 408 is used to control the opening or closing of the second pipeline assembly 403 to control the flow state of the liquid carbon dioxide in the second pipeline assembly 403 .

[0119] like Figure 4 As shown, the third pipeline assembly 404 provided in the embodiment of the present application is provided with a first throttle valve 4041, and the first throttle valve 4041 is used to communicate with the bottom outlet side of the cold distillation tower 401 and the top condenser 406 respectively through the third pipeline assembly 404; the first pipeline assembly 402 includes a first sub-pipeline 4021 and a second sub-pipeline 4022, and the fourth pipeline assembly 405 includes a third sub-pipeline 4051 and a fourth sub-pipeline 4052; the first sub-pipeline 4021 is provided with a waste cooling heat exchanger 407, and is thermally connected to the third sub-pipeline 4051, the second sub-pipeline 4022 is provided with a refrigeration system heat exchanger 309, and is thermally connected to the second pipeline assembly 403, and the fourth sub-pipeline 4052 is connected to the outlet of the compression device 200.

[0120] It can be understood that, in the process that the fluid on the bottom outlet side of the cold distillation tower 401 can pass through the third pipeline assembly 404 and then enter the top condenser 406, the liquid carbon dioxide in the fluid on the bottom outlet side of the cold distillation tower 401 can pass through the first throttle valve 4041. The first throttle valve 4041 is used to gasify the liquid carbon dioxide so that the temperature of the fluid transported to the top condenser 406 by the third pipeline assembly 404 is reduced, thereby providing a low temperature environment for the top condenser 406, which can improve the cold capacity utilization rate of the liquid carbon dioxide entering the third pipeline assembly 404.

[0121] It can be understood that the third sub-pipeline 4051 is used to guide the low-temperature nitrogen in the tower top condenser 406 to the next process or the external environment.

[0122] It can be understood that the fourth sub-pipeline 4052 is used to guide the fluid in the tower top condenser 406 to the compression device 200 to recycle the fluid in the tower top condenser 406, thereby improving the yield of liquid carbon dioxide in the carbon capture system.

[0123] It should be noted that the connection between the third sub-pipeline 4051 and the top condenser 406 is located above the connection between the fourth sub-pipeline 4052 and the top condenser 406, so that the lighter nitrogen in the upper layer can be exported to the next process or the external environment through the third sub-pipeline 4051, thereby reducing the waste of fluid in the condenser 302 and pollution to the environment.

[0124] It can be understood that the setting of the waste cooling heat exchanger 407 can make the first sub-pipeline 4021 and the third sub-pipeline 4051 thermally conductive, so that the low-temperature nitrogen in the third sub-pipeline 4051 can exchange heat with the fluid in the first sub-pipeline 4021 to reduce the temperature of the fluid in the first sub-pipeline 4021, so that the fluid entering the cold distillation tower 401 can be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and can improve the cold utilization rate of the refrigeration device 300, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0125] It can be understood that a refrigeration system heat exchanger 309 is provided on the second sub-pipeline 4022 and is thermally connected to the refrigeration device 300, so that the refrigeration device 300 can exchange heat with the fluid in the second sub-pipeline 4022 to reduce the temperature of the fluid in the second sub-pipeline 4022, so that the fluid entering the cold distillation tower 401 can be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and the cold utilization rate of the refrigeration device 300 can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0126] It should be noted that the refrigeration device 300 includes: a refrigeration distillation tower 301, a condenser 302, a reboiler 303, an ammonia cooler 304, a liquid ammonia buffer tank 305, a concentrated ammonia preheater 306, an ammonia absorption tank 307, and a second throttle valve 308; the refrigeration distillation tower 301, the ammonia cooler 304, the liquid ammonia buffer tank 305, the second throttle valve 308 and the concentrated ammonia preheater 306 are connected in sequence through pipelines; the refrigeration distillation tower 301 is connected to the condenser 302 through a first connecting pipe; the reboiler 303 is connected to The refrigeration distillation tower 301 is connected via a second connecting pipe; the concentrated ammonia water preheater 306 is connected to the refrigeration distillation tower 301 via a third connecting pipe; the liquid ammonia buffer tank 305 and the ammonia absorption tank 307 are connected via a pipeline to form a refrigeration end of the refrigeration device 300, and the throttle valve is located at the refrigeration end; a portion of the pipeline at the refrigeration end is thermally connected to the second sub-pipeline 4022 via the refrigeration system heat exchanger 309; and / or another portion of the pipeline at the refrigeration end is thermally connected to the second pipeline assembly 403 via the product heat exchanger 3010.

[0127] It can be understood that the refrigeration device 300 is used to cool the carbon-containing gas so that part of the gas in the carbon-containing gas can be liquefied and the other part of the gas in the carbon-containing gas remains in a gaseous state.

[0128] It should be noted that the carbon-containing gas entering the refrigeration device 300 mainly includes: carbon dioxide gas and nitrogen, wherein the liquefaction temperature of carbon dioxide is -78.5°C, and the liquefaction temperature of nitrogen is -195.8°C. The carbon dioxide in the carbon-containing gas entering the refrigeration device 300 is liquefied first.

[0129] It should be noted that the pipeline located in the refrigeration end has a variety of different heat conduction positions, and the heat conduction positions of the pipeline located in the refrigeration end are described below with examples one by one.

[0130] In a feasible implementation manner, a portion of the pipeline located at the refrigeration end is thermally connected to the second sub-pipeline 4022 through the refrigeration system heat exchanger 309 .

[0131] It can be understood that the refrigeration system heat exchanger 309 is thermally connected to the refrigeration end and the second sub-pipeline 4022, respectively, so that the refrigeration end can exchange heat with the fluid in the second sub-pipeline 4022 to reduce the temperature of the fluid in the second sub-pipeline 4022, so that the fluid entering the cold distillation tower 401 can be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and the cold utilization rate of the refrigeration device 300 can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage.

[0132] In another feasible implementation, another portion of the pipeline located at the refrigeration end is thermally connected to the second pipeline assembly 403 through the product heat exchanger 3010.

[0133] It can be understood that the product heat exchanger 3010 is thermally connected to the refrigeration end and the second pipeline assembly 403 respectively, so that the cryogenic liquid carbon dioxide in the second pipeline assembly 403 can generate heat exchange with the refrigeration end to reduce the surface temperature of the refrigeration end, thereby improving the utilization rate of the cryogenic liquid carbon dioxide in the second pipeline assembly 403.

[0134] In addition, in another feasible embodiment, a portion of the pipeline at the refrigeration end is thermally connected to the second sub-pipeline 4022 through the refrigeration system heat exchanger 309, and another portion of the pipeline at the refrigeration end is thermally connected to the second pipeline assembly 403 through the product heat exchanger 3010. The product heat exchanger 3010 is located on a side of the refrigeration system heat exchanger 309 away from the ammonia absorption tank 307.

[0135] It can be understood that the refrigeration system heat exchanger 309 is thermally connected with the refrigeration end and the second sub-pipeline 4022, respectively, so that the refrigeration end can exchange heat with the fluid in the second sub-pipeline 4022 to reduce the temperature of the fluid in the second sub-pipeline 4022, so that the fluid entering the cold distillation tower 401 can be pre-cooled to reduce the cold consumption of the cold distillation tower 401, and the cold utilization rate of the refrigeration device 300 can be improved, thereby improving the energy utilization rate of carbon dioxide capture, utilization and storage. The product heat exchanger 3010 is thermally connected with the refrigeration end and the second pipeline assembly 403, respectively, so that the low-temperature liquid carbon dioxide in the second pipeline assembly 403 can exchange heat with the refrigeration end to reduce the surface temperature of the refrigeration end, thereby improving the utilization rate of the low-temperature liquid carbon dioxide in the second pipeline assembly 403. The product heat exchanger 3010 is located on the side of the refrigeration system heat exchanger 309 away from the ammonia absorption tank 307, so that the cold energy transported to the refrigeration end by the low-temperature liquid carbon dioxide in the second pipeline assembly 403 can be exchanged to the second sub-pipeline 4022 after passing through the refrigeration system heat exchanger 309, thereby reducing the temperature of the fluid in the second sub-pipeline 4022 and improving the utilization rate of the cold energy in the second pipeline assembly 403.

[0136] It should be noted that in the process of concentrating ammonia water in the refrigeration distillation tower 301, ammonia gas with a pressure of 1.3 to 1.8 MPa is produced at the top of the tower, while dilute ammonia water with an ammonia mass concentration of 8 to 24% is produced at the bottom of the tower; subsequently, the high-pressure ammonia gas is cooled to 35°C through the condenser 302 and becomes liquid ammonia, and then the pressure is reduced to 0.1 to 0.4 MPa through the throttle valve. The gas-liquid mixed ammonia converted in this process can be used to cool the high-purity CO2 fluid; after the refrigeration is completed, the ammonia gas is mixed with the dilute ammonia water at the bottom of the tower to form concentrated ammonia water, and is sent to the refrigeration distillation tower 301 as feed after preheating.

[0137] The denitrification and desulfurization device 100 provided in the embodiment of the present application includes a denitrification component 101 and a desulfurization component 102. It should be noted that there are many different connection methods between the denitrification component 101 and the desulfurization component 102. The connection methods between the denitrification component 101 and the desulfurization component 102 are illustrated below in turn.

[0138] In a feasible embodiment, the inlet end of the denitrification component 101 is used for introducing carbon-containing exhaust gas, the outlet end of the denitrification component 101 is connected to the inlet end of the desulfurization component 102 through a pipeline, and the outlet end of the desulfurization component 102 is connected to the inlet of the compression device 200 through another pipeline.

[0139] In another feasible embodiment, the inlet end of the desulfurization component 102 is used for introducing carbon-containing exhaust gas, the outlet end of the desulfurization component 102 is connected to the inlet end of the denitrification component 101 through a pipeline, and the outlet end of the denitrification component 101 is connected to the inlet of the compression device 200 through another pipeline.

[0140] It is understandable that there is no restriction on the connection method between the denitration component 101 and the desulfurization component 102, and it can be selected according to actual use requirements.

[0141] It should be noted that the denitrification component 101 is used to remove nitrogen oxides from the carbon-containing exhaust gas, and the desulfurization component 102 is used to remove sulfur dioxide gas from the carbon-containing exhaust gas to improve the yield rate of the finished liquid carbon dioxide of the carbon capture system.

[0142] It should be noted that the desulfurization component 102 provided in the embodiment of the present application includes a venturi chiller 1021 , the inlet of the venturi chiller 1021 forms the inlet side of the denitrification and desulfurization device 100 , and the outlet of the venturi chiller 1021 is connected to the denitrification component 101 .

[0143] It can be understood that the carbon-containing waste gas is blown into the venturi chiller 1021 under positive pressure through the induced draft fan, and the sulfur dioxide gas in the carbon-containing waste gas reacts with the atomized alkaline solution sodium hydroxide droplets in the venturi chiller 1021 to generate sodium sulfate as a by-product, so as to achieve the removal of sulfur dioxide gas in the carbon-containing waste gas.

[0144] It should be noted that the denitrification component 101 includes an SCR reactor 1011 and a waste heat boiler 1012. The inlet of the waste heat boiler 1012 forms the inlet side of the denitrification and desulfurization device 100. The outlet of the waste heat boiler 1012 is connected to the inlet of the SCR reactor 1011, and the outlet of the SCR reactor 1011 is connected to the desulfurization component 102.

[0145] It can be understood that the SCR reactor 1011 can be an SCR reactor 1011, which uses ammonia in the SCR reactor 1011 as a catalyst and uses oxygen to reduce nitrogen oxides in the carbon-containing exhaust gas to nitrogen and water at a reaction temperature of 120°C-300°C, so as to remove nitrogen oxides in the carbon-containing exhaust gas.

[0146] It should be noted that the use of the waste heat boiler 1012 can preheat the carbon-containing exhaust gas to reduce the heating energy consumption of the SCR reactor 1011.

[0147] An embodiment of the present application provides a carbon capture method, which is applied to the carbon capture system provided in any of the above embodiments. The carbon capture method includes:

[0148] Desulfurization and denitration treatment, passing the carbon-containing waste gas into the denitration and desulfurization device 100 to remove at least part of the sulfur dioxide gas and a small part of nitrogen oxides in the carbon-containing waste gas, and obtain a first gas;

[0149] Compression treatment, passing the first gas through a three-stage compression assembly to remove water vapor in the first gas and obtain a second gas;

[0150] Cooling treatment, using a refrigeration device 300 to cool the second gas, so that at least part of the second gas is liquefied to form a gas-liquid mixture;

[0151] Cold distillation treatment, passing the gas-liquid mixture into a cold distillation tower 401 to separate the gas and liquid in the gas-liquid mixture to obtain a low-temperature and high-pressure first liquid and a low-temperature third gas;

[0152] Heat exchange treatment is performed to conduct heat between the low-temperature and high-pressure first liquid and the refrigeration device 300 to obtain the first liquid at room temperature and high pressure, and / or, heat conduction is performed between the low-temperature third gas and the refrigeration device 300 to obtain the third gas at room temperature.

[0153] It can be understood that the denitration and desulfurization treatment is used to remove nitrogen oxides and sulfur dioxide in the carbon-containing gas, the compression treatment is used to remove water vapor in the carbon-containing gas, the cooling treatment is used to cool the carbon-containing gas so that part of the gas in the carbon-containing gas can be liquefied, and the cold distillation treatment is used to perform cold distillation treatment on the liquefied part of the gas and the unliquefied gas so that the carbon dioxide in the liquefied part of the gas and the unliquefied gas can be liquefied into liquid carbon dioxide, thereby separating the liquid carbon dioxide from the nitrogen. The heat exchange treatment is used to improve the utilization rate of the cold between the compression component and the cold distillation tower 401, so as to improve the energy utilization rate of carbon dioxide capture, utilization and storage.

[0154] It should be noted that there are many different ways to set up the heat exchange treatment, and the following will illustrate the ways to set up the heat exchange treatment in turn with examples.

[0155] In a feasible implementation, the heat exchange process may be to heat-exchange the first liquid at low temperature and high pressure to the refrigeration device 300 to obtain the first liquid at room temperature and high pressure.

[0156] It is understandable that the low-temperature and high-pressure first liquid is connected to the refrigeration device 300 so that the cold energy of the first liquid can be transferred to the refrigeration device 300 to improve the utilization rate of the cold energy of the first liquid.

[0157] In another feasible implementation, the heat exchange process may be to conduct heat between the low-temperature third gas and the refrigeration device 300 to obtain the third gas at room temperature.

[0158] It is understandable that thermal conduction between the low-temperature third gas and the refrigeration device 300 can increase the coldness of the low-temperature third gas that can be transferred to the refrigeration device 300, thereby improving the coldness utilization rate of the low-temperature third gas.

[0159] It should be noted that there are many different methods for setting up desulfurization and denitrification treatment. The following examples will be used to illustrate the methods for setting up desulfurization and denitrification treatment.

[0160] In a feasible implementation manner, the desulfurization and denitrification treatment is:

[0161] Pretreatment: The carbon-containing waste gas is passed into the waste heat boiler 1012 to cool the carbon-containing waste gas to 100°C-200°C;

[0162] Denitration: passing the carbon-containing waste gas at 100° C. to 200° C. into the denitration component 101 to remove at least part of the nitrogen oxides in the carbon-containing waste gas and obtain a first pretreated gas;

[0163] Desulfurization: The first pretreated gas is introduced into the desulfurization component 102 to remove at least a portion of sulfur dioxide gas in the first pretreated gas to obtain the first gas.

[0164] It is understood that pretreatment can improve the heat utilization of carbon-containing exhaust gas to reduce the processing cost of liquid carbon dioxide for carbon capture.

[0165] In another feasible implementation, the desulfurization and denitrification treatment is:

[0166] Desulfurization: passing the carbon-containing waste gas into the desulfurization component 102 to remove at least part of the sulfur dioxide gas in the carbon-containing waste gas and obtain a second pretreated gas;

[0167] Denitration: The second pre-treated gas is introduced into the denitration component 101 to remove at least part of nitrogen oxides in the second pre-treated gas to obtain the first gas.

[0168] It is understandable that desulfurization and denitrification can reduce the difficulty of implementing the carbon capture method to improve the operational convenience of the carbon capture method.

[0169] It should be noted that the phrases "one embodiment", "an embodiment", "an exemplary embodiment", "some embodiments", etc. mentioned in the specification indicate that the described embodiments may include certain features, structures or characteristics, but not every embodiment may include the certain features, structures or characteristics. In addition, such phrases do not necessarily refer to the same embodiment. In addition, when describing certain features, structures or characteristics in conjunction with an embodiment, it is within the knowledge of those skilled in the art to implement such features, structures or characteristics in conjunction with other embodiments, whether explicitly or not explicitly described.

[0170] In general, terms should be understood, at least in part, by the context in which they are used. For example, the term "one or more" as used herein may be used to describe any feature, structure, or characteristic in a singular sense, or may be used to describe a combination of features, structures, or characteristics in a plural sense, depending, at least in part, on the context. Similarly, terms such as "a," "an," or "the" may also be understood to convey singular usage or to convey plural usage, depending, at least in part, on the context.

[0171] It should be easily understood that “on,” “above,” and “over” in this application should be interpreted in the broadest manner, so that “on” not only means “directly on something,” but also includes the meaning of “on something” with intervening features or layers therebetween, and “above” or “over” not only includes the meaning of “above something” or “over,” but also may include the meaning of “above something” or “over” with no intervening features or layers therebetween (i.e., directly on something).

[0172] In addition, spatially relative terms, such as "below," "below," "below," "above," "above," etc., may be used herein for ease of description to describe the relationship of one element or feature relative to other elements or features as shown in the figures. Spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation shown in the figures. The device may have other orientations (rotated 90° or at other orientations), and the spatially relative descriptors used herein may likewise be interpreted accordingly.

[0173] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit it. Although the present application has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A carbon capture system, characterized in that: include: A denitration and desulfurization device (100), a compression device (200), a refrigeration device (300) and a cold distillation device (400), wherein the inlet side of the denitration and desulfurization device (100) is used to introduce carbon-containing waste gas; The denitration and desulfurization device (100), the compression device (200) and the cold distillation device (400) are connected in sequence through pipelines, and the pipeline between the compression device (200) and the cold distillation device (400) is thermally connected to the refrigeration end of the refrigeration device (300); The cold distillation device (400) comprises a cold distillation tower (401), and at least one of an inlet side and an outlet side of the cold distillation tower (401) is thermally connected to a refrigeration end of the refrigeration device (300).

2. A carbon capture system according to claim 1, characterized in that: The compression device (200) has an inlet and an outlet. The inlet of the compression device (200) is connected to the outlet of the denitration and desulfurization device (100) through one of the pipelines, and the outlet of the compression device (200) is connected to the inlet side of the cold distillation tower (401) through another of the pipelines.

3. A carbon capture system according to claim 2, characterized in that: The cold distillation device (400) further comprises a first pipeline assembly (402), a second pipeline assembly (403), a third pipeline assembly (404), a fourth pipeline assembly (405) and a tower top condenser (406), wherein the tower top condenser (406) is arranged at the outlet side of the cold distillation tower (401); The inlet side of the cold distillation tower (401) is connected to the outlet of the compression device (200) through the first pipeline assembly (402); The bottom outlet side of the cold distillation tower (401) is thermally connected to the refrigeration end of the refrigeration device (300) through the second pipeline assembly (403); The bottom outlet side of the cold distillation tower (401) is connected to the top condenser (406) through the third pipeline assembly (404); The outlet side of the tower top condenser (406) is connected to at least the compression device (200) through the fourth pipeline assembly (405).

4. A carbon capture system according to claim 3, characterized in that: The third pipeline assembly (404) is provided with a first throttle valve (4041), and the first throttle valve (4041) is used to communicate with the bottom outlet side of the cold distillation tower (401) and the top condenser (406) through the third pipeline assembly (404); The first pipeline assembly (402) includes a first sub-pipeline (4021) and a second sub-pipeline (4022), and the fourth pipeline assembly (405) includes a third sub-pipeline (4051) and a fourth sub-pipeline (4052); the first sub-pipeline (4021) is provided with a residual cooling heat exchanger (407) and is thermally connected to the third sub-pipeline (4051); the second sub-pipeline (4022) is provided with a refrigeration system heat exchanger (309) and is thermally connected to the second pipeline assembly (403); and the fourth sub-pipeline (4052) is connected to the outlet of the compression device (200).

5. A carbon capture system according to claim 4, characterized in that: The refrigeration device (300) comprises a refrigeration distillation tower (301), a condenser (302), a reboiler (303), an ammonia cooler (304), a liquid ammonia buffer tank (305), a concentrated ammonia water preheater (306), an ammonia absorption tank (307), and a second throttle valve (308); The refrigeration distillation tower (301), the ammonia cooler (304), the liquid ammonia buffer tank (305), the second throttle valve (308) and the concentrated ammonia water preheater (306) are connected in sequence through the pipeline; The refrigeration distillation tower (301) is connected to the condenser (302) via a first connecting pipe; The reboiler (303) is connected to the refrigeration distillation tower (301) via a second connecting pipe; The concentrated ammonia water preheater (306) is connected to the refrigeration distillation tower (301) via a third connecting pipe; The liquid ammonia buffer tank (305) and the ammonia absorption tank (307) are connected via the pipeline to form a refrigeration end of the refrigeration device (300), and the throttle valve is located at the refrigeration end; A portion of the pipeline located at the refrigeration end is thermally connected to the second sub-pipeline (4022) via the refrigeration system heat exchanger (309); And / or, another part of the pipeline at the refrigeration end is thermally connected to the second pipeline assembly (403) through the product heat exchanger (3010).

6. A carbon capture system according to any one of claims 1 to 5, characterized in that: The denitration and desulfurization device (100) comprises a denitration component (101) and a desulfurization component (102), wherein the inlet end of the denitration component (101) is used for introducing carbon-containing waste gas, the outlet end of the denitration component (101) is connected to the inlet end of the desulfurization component (102) through one of the pipelines, and the outlet end of the desulfurization component (102) is connected to the inlet of the compression device (200) through another of the pipelines; Alternatively, the inlet end of the desulfurization component (102) is used for introducing carbon-containing exhaust gas, the outlet end of the desulfurization component (102) is connected to the inlet end of the denitrification component (101) through one of the pipelines, and the outlet end of the denitrification component (101) is connected to the inlet of the compression device (200) through another of the pipelines.

7. A carbon capture system according to claim 6, characterized in that: The desulfurization component (102) comprises a venturi chiller (1021), the inlet of the venturi chiller (1021) forms the inlet side of the denitration and desulfurization device (100), and the outlet of the venturi chiller (1021) is in communication with the denitration component (101); And / or, the denitration component (101) includes an SCR reactor (1011) and a waste heat boiler (1012), the inlet of the waste heat boiler (1012) forms the inlet side of the denitration and desulfurization device (100), the outlet of the waste heat boiler (1012) is connected to the inlet of the SCR reactor (1011), and the outlet of the SCR reactor (1011) is connected to the desulfurization component (102).

8. A carbon capture system according to any one of claims 1 to 5, characterized in that: The compression device (200) is a three-stage compression assembly, one end of which is connected to the denitration and desulfurization device (100), and the other end of which is connected to the cold distillation tower (401).

9. A carbon capture method, characterized in that: A carbon capture system according to any one of claims 1 to 8, wherein the carbon capture method comprises: Desulfurization and denitration treatment, passing the carbon-containing waste gas into a denitration and desulfurization device (100) to remove at least part of sulfur dioxide gas and a small part of nitrogen oxides in the carbon-containing waste gas, and obtain a first gas; Compression treatment, passing the first gas through a three-stage compression assembly to remove water vapor in the first gas and obtain a second gas; Cooling the second gas using a refrigeration device (300) to cool the second gas so that at least part of the second gas is liquefied to form a gas-liquid mixture; Cold distillation treatment, passing the gas-liquid mixture into a cold distillation tower (401) to separate the gas and liquid in the gas-liquid mixture to obtain a low-temperature and high-pressure first liquid and a low-temperature third gas; Heat exchange treatment is performed to conduct heat between the first liquid at low temperature and high pressure and the refrigeration device (300) to obtain the first liquid at room temperature and high pressure, and / or, heat conduction is performed between the third gas at low temperature and the refrigeration device (300) to obtain the third gas at room temperature.

10. A carbon capture method according to claim 9, characterized in that: Desulfurization and denitrification treatment includes: Pretreatment: passing the carbon-containing waste gas into a waste heat boiler (1012) to cool the carbon-containing waste gas to 100°C-200°C; Denitration: passing the carbon-containing waste gas at 100° C. to 200° C. into a denitration component (101) to remove at least part of nitrogen oxides in the carbon-containing waste gas and obtain a first pretreated gas; Desulfurization: passing the first pretreated gas into a desulfurization component (102) to remove at least part of sulfur dioxide gas in the first pretreated gas to obtain the first gas; Or, desulfurization: passing the carbon-containing waste gas into the desulfurization component (102) to remove at least part of the sulfur dioxide gas in the carbon-containing waste gas and obtain a second pretreated gas; Denitration: The second pretreated gas is introduced into a denitration component (101) to remove at least part of nitrogen oxides in the second pretreated gas to obtain the first gas.

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