A trap device and a trapping method

Abstract

The application relates to the technical field of carbon dioxide capture, and provides a capture device and a capture method, the capture device comprising a preheating assembly, a calcination furnace, a separation assembly, a spray tower, a liquefaction assembly, a collection assembly and a stripping tower, wherein the inlet of the calcination furnace is communicated with the outlet of the preheating assembly, the inlet of the separation assembly is communicated with the outlet of the calcination furnace, the inlet of the spray tower is communicated with the outlet of the separation assembly, the inlet of the liquefaction assembly is communicated with the outlet of the spray tower, the liquefaction assembly is in thermal conduction connection with the separation assembly, the collection assembly is communicated with the separation assembly, and the stripping tower is communicated with the liquefaction assembly. The application can solve the problem that it is difficult to capture carbon dioxide.

Description

Technical Field

[0001] This application relates to the field of carbon dioxide capture technology, and in particular to a capture device and capture method. Background Technology

[0002] In alumina production, the final step is to calcine aluminum hydroxide at high temperature to remove moisture and generate metallurgical-grade alumina suitable for electrolysis. Specifically, during the calcination of aluminum hydroxide, it decomposes into alumina and water vapor upon heating, while carbon dioxide emissions are also produced during fuel combustion.

[0003] In related technologies, in order to reduce carbon emissions, it is necessary to capture the carbon dioxide generated by combustion. Carbon dioxide capture technology is used to remove carbon dioxide from the gas stream or separate carbon dioxide as a gaseous product.

[0004] However, there are difficulties in capturing carbon dioxide. Summary of the Invention

[0005] This application provides a capture device and a capture method that can solve the problem of high capture difficulty when capturing carbon dioxide.

[0006] To achieve the above objectives, this application adopts the following technical solution:

[0007] In a first aspect, this application provides a collection device, comprising:

[0008] Preheating components;

[0009] The roasting furnace has its inlet connected to the outlet of the preheating components;

[0010] The separation component has its inlet connected to the outlet of the roasting furnace;

[0011] The spray tower has its inlet connected to the outlet of the separation component;

[0012] The liquefaction component has its inlet connected to the outlet of the spray tower, and it is thermally connected to the separation component.

[0013] Collect components and connect them to separate components;

[0014] The stripping tower is connected to the liquefaction unit.

[0015] In some embodiments, the roasting furnace has a first inlet, a second inlet, and a third inlet connected together, the third inlet being used for external gas supply;

[0016] The preheating components include:

[0017] The gas source pipeline has one end for connecting to an external oxygen delivery device and the other end connected to the first inlet.

[0018] The preheater is connected to the gas source pipeline.

[0019] In some implementations, the separation component includes:

[0020] The first separator has its inlet connected to the outlet of the roasting furnace, and its solid outlet connected to the gas source pipeline.

[0021] The second separator has its inlet connected to the gas outlet of the first separator, and its solid outlet connected to the second inlet.

[0022] The third separator has its inlet connected to the gas outlet of the second separator, and its solid outlet connected to the gas outlet of the first separator and the inlet of the second separator, respectively.

[0023] The dust collector has its inlet connected to the gas outlet of the third separator, its gas outlet connected to the inlet of the spray tower, and its solid outlet connected to the gas source pipeline.

[0024] In some implementations, it also includes:

[0025] The conveying pipeline has one end connected to an external aluminum hydroxide conveying device and the other end connected to the inlet of the third separator.

[0026] In some implementations, the outlet of the spray tower is connected to the gas source pipeline;

[0027] The liquefaction components include:

[0028] The compressor component has its inlet connected to the outlet of the spray tower.

[0029] The compressor and the air supply pipeline are connected in parallel.

[0030] In some embodiments, the liquefaction component further includes:

[0031] The dehydration component has its inlet connected to the outlet of the compression component;

[0032] The cooler has its inlet connected to the outlet of the dehydration unit, and its outlet connected to the inlet of the stripping tower.

[0033] In some embodiments, the liquefaction component further includes:

[0034] An evaporator has a first heat exchange pipeline and a second heat exchange pipeline connected by heat conduction. The first heat exchange pipeline is connected to the gas outlet of the first separator and the inlet of the second separator, respectively.

[0035] A distillation column has an inner cavity and a fourth inlet, a first outlet, a fifth inlet, and a second outlet that are respectively connected to the inner cavity. The inner cavity is used to contain the cooling medium. Along the height of the distillation column, the second outlet, the fifth inlet, the fourth inlet, and the first outlet are arranged at intervals, with the second outlet located at the top of the distillation column and the first outlet located at the bottom of the distillation column.

[0036] The second heat exchange pipeline is connected to the fourth inlet and the first outlet, respectively;

[0037] The cooler has a third heat exchange pipeline and a fourth heat exchange pipeline connected by heat conduction. The third heat exchange pipeline is connected to the outlet of the dehydration unit and the inlet of the stripping tower, respectively. The fourth heat exchange pipeline is connected to the fifth inlet and the second outlet, respectively.

[0038] A throttle valve is connected between the second outlet and the cooler.

[0039] In some embodiments, the stripping tower has a third outlet, a sixth inlet, and a seventh inlet connected together, with the third outlet located at the bottom of the stripping tower, the sixth inlet located at the top of the stripping tower, and the seventh inlet connected to the outlet of the cooler.

[0040] The sixth import includes the first sub-import, the second sub-import, and the third sub-import, which are connected in parallel.

[0041] The third outlet is used to connect to an external carbon dioxide collection device, and the third outlet is connected to the first sub-inlet;

[0042] The second sub-inlet is connected to the inlet of the dehydration unit;

[0043] The third sub-inlet is connected to the inlet of the compression component.

[0044] In some implementations, the collection component includes:

[0045] The output pipeline connects to the outlet of the preheater;

[0046] The heat exchanger is connected to the output pipeline.

[0047] Secondly, this application provides a collection method applied to a collection device, comprising the following steps:

[0048] The material is fed into the preheating component and preheated by the preheating component;

[0049] The preheated material is conveyed to the roasting furnace, where it is burned to produce separated products.

[0050] The separation products are conveyed to a separation unit, where they are separated into gaseous and solid products.

[0051] The gaseous products are transported to a spray tower, which is used to clean the gaseous products.

[0052] The cleaned gaseous product is conveyed to the liquefaction unit, which pressurizes and cools the cleaned gaseous product to convert it into a liquid product and remove moisture; the separation unit also provides a heat source to the liquefaction unit.

[0053] The cooled gaseous products are then transported to a stripping tower.

[0054] Solid products are transported to the collection component.

[0055] This collection device, through the inclusion of a preheating component, preheats the material to ensure a uniform temperature rise. A roasting furnace further heats the preheated material, allowing it to burn and generate separation products. These products are then conveyed to a separation component, where they are separated into gaseous and solid phases. The separated gaseous products are then transported to a spray tower for cleaning before being conveyed to a liquefaction component. The liquefaction component cools the cleaned gaseous products, which are then conveyed to a stripping tower for further collection. The separated solid products are then conveyed to a collection component for final collection. By thermally connecting the liquefaction and separation components, heat exchange occurs between them. This allows the separation component to cool the separated products while simultaneously providing heat to the liquefaction component, further reducing the workload of the spray tower and liquefaction component in subsequent processes and improving the heat utilization rate of the separated products.

[0056] Therefore, this application can solve the problem of high difficulty in capturing carbon dioxide. Attached Figure Description

[0057] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0058] Figure 1 This is a schematic diagram of the main structure of the trapping device provided in the embodiments of this application;

[0059] Figure 2 A flowchart of the capture method provided in the embodiments of this application.

[0060] Explanation of reference numerals in the attached figures:

[0061] 100 - Preheating assembly; 101 - Gas supply pipeline; 102 - Preheater;

[0062] 200-roasting oven;

[0063] 300 - Separation assembly; 301 - First separator; 302 - Second separator; 303 - Third separator; 304 - Dust collector;

[0064] 400-Spray Tower;

[0065] 500 - Liquefaction assembly; 501 - Compressor; 502 - Dehydrator; 503 - Cooler; 504 - Evaporator; 505 - Distillation column; 506 - Throttling valve;

[0066] 600 - Collection assembly; 601 - Output pipeline; 602 - Heat exchanger;

[0067] 700-Stripping Tower;

[0068] 800 - Delivery pipeline. Detailed Implementation

[0069] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application. Unless otherwise specified, the following embodiments and features can be combined with each other.

[0070] In the existing technology, traditional roasting furnaces use air as the combustion medium. However, air has a high nitrogen content, so the flue gas after combustion in the roasting furnace contains a large volume of nitrogen, which results in a very low concentration of carbon dioxide in the flue gas.

[0071] This leads to difficulties in capturing carbon dioxide.

[0072] To overcome the shortcomings of existing technologies, a preheating component is incorporated to preheat the material, ensuring a uniform temperature rise. A roasting furnace is then installed to further heat the preheated material, allowing it to burn and generate separation products. These products are then conveyed to a separation component, where they are separated into gaseous and solid products. The separated gaseous products are transported to a spray tower for cleaning and then to a liquefaction component for cooling. The cooled gaseous products are then conveyed to a stripping tower for collection. The separated solid products are conveyed to a collection component for collection. By thermally connecting the liquefaction and separation components, heat exchange is possible. This allows the separation component to cool the products within its own component while simultaneously providing heat to the liquefaction component, further cooling the products and reducing the workload of the spray tower and liquefaction component in subsequent processes. It also improves the heat utilization rate of the separated products.

[0073] Therefore, this application can solve the problem of high difficulty in capturing carbon dioxide.

[0074] The contents of this application will now be described in detail with reference to the accompanying drawings, so that those skilled in the art can have a clearer and more detailed understanding of the contents of this application.

[0075] like Figure 1 As shown, this application provides a collection device, including a preheating component 100, a roasting furnace 200, a separation component 300, a spray tower 400, a liquefaction component 500, a collection component 600, and a stripping tower 700. The inlet of the roasting furnace 200 is connected to the outlet of the preheating component 100, the inlet of the separation component 300 is connected to the outlet of the roasting furnace 200, the inlet of the spray tower 400 is connected to the outlet of the separation component 300, the inlet of the liquefaction component 500 is connected to the outlet of the spray tower 400, the liquefaction component 500 and the separation component 300 are thermally connected, the collection component 600 is connected to the separation component 300, and the stripping tower 700 is connected to the liquefaction component 500.

[0076] The following sections provide a detailed description of the specific structure of the collection device and collection method, as well as various possible implementation methods.

[0077] The roasting furnace 200 provided in the embodiments of this application has a first inlet, a second inlet and a third inlet connected together. The third inlet is used to connect to external gas. The preheating component 100 includes a gas source pipeline 101 and a preheater 102. One end of the gas source pipeline 101 is used to connect to an external oxygen delivery device, and the other end of the gas source pipeline 101 is connected to the first inlet. The preheater 102 is connected to the gas source pipeline 101.

[0078] It is understood that, through the above-described embodiments, oxygen in the oxygen delivery device can be delivered to the calcining furnace 200 via the gas source pipeline 101 and the first inlet, and fuel gas can be delivered to the calcining furnace 200 via the third inlet. In the calcining furnace 200, the fuel gas and oxygen can be used for combustion to generate high temperatures, so that aluminum hydroxide can be decomposed under high temperature conditions. In addition, oxygen replacing air as a combustion aid can make the combustion products mainly carbon dioxide and water, thereby reducing the volume and content of nitrogen in the flue gas after combustion, thereby increasing the carbon dioxide content in the flue gas, which facilitates the capture of carbon dioxide.

[0079] It should be noted that the preheater 102 can be a 2-6 stage cyclone device or a 3-4 stage cyclone device. There are no restrictions here, and it can be selected according to the actual use requirements.

[0080] It should be noted that the gas can be hydrogen, carbon monoxide, methane, propane, butane, or a combination of one or more of the above gases. There are no restrictions, and the gas can be selected according to actual usage requirements.

[0081] The separation component 300 provided in the embodiments of this application includes: a first separator 301, a second separator 302, a third separator 303, and a dust removal component 304. The inlet of the first separator 301 is connected to the outlet of the roasting furnace 200, and the solid outlet of the first separator 301 is connected to the gas source pipeline 101. The inlet of the second separator 302 is connected to the gas outlet of the first separator 301, and the solid outlet of the second separator 302 is connected to the second inlet. The inlet of the third separator 303 is connected to the gas outlet of the second separator 302, and the solid outlet of the third separator 303 is connected to both the gas outlet of the first separator 301 and the inlet of the second separator 302. The inlet of the dust removal component 304 is connected to the gas outlet of the third separator 303, the gas outlet of the dust removal component 304 is connected to the inlet of the spray tower 400, and the solid outlet of the dust removal component 304 is connected to the gas source pipeline 101.

[0082] It is understood that, through the above-described embodiments, the exhaust gas from the combustion in the calcining furnace 200 can be sequentially transported to the spray tower 400 after passing through the first separator 301, the second separator 302, the third separator 303, and the dust collector 304. This reduces the content of solid products in the flue gas entering the spray tower 400. The solid products separated by the first separator 301 can be reintroduced into the calcining furnace 200 through the gas source pipeline 101 and the first inlet, thereby allowing for the re-decomposition of incompletely decomposed aluminum hydroxide, or the solid products separated by the first separator 301... Solid products can enter the preheater 102 through the gas source pipeline 101 and be further discharged through the output pipeline 601 to collect alumina. Solid products separated by the second separator 302 can be transported to the calcining furnace 200 through the second inlet to collect solid products. Solid products separated by the third separator 303 can be transported to the second separator 302 through the inlet of the second separator 302 and separated again by the second separator 302. Solid products passing through the dust removal component 304 can be transported to the gas source pipeline 101.

[0083] It should be noted that the solid product is aluminum hydroxide, aluminum oxide, dust, or a mixture of at least two of the above three, and there are no restrictions on this.

[0084] It should be noted that the first separator 301 can be a first cyclone separator, a first electrostatic precipitator, or other equipment that can separate gas and solids. There are no restrictions here, and it can be selected according to actual usage requirements.

[0085] It should be noted that the second separator 302 can be a second cyclone separator, a second electrostatic precipitator, or other equipment that can separate gas and solids. There are no restrictions here, and it can be selected according to actual usage requirements.

[0086] It should be noted that the third separator 303 can be a third cyclone separator, a third electrostatic precipitator, or other equipment that can separate gas and solids. There are no restrictions here, and it can be selected according to actual usage requirements.

[0087] It should be noted that the dust removal component 304 can be an electrostatic precipitator, a bag filter, a wet electrostatic precipitator, or other equipment that can separate gas and solids. There are no restrictions here, and it can be selected according to the actual use requirements.

[0088] The collection device provided in the embodiments of this application further includes: a conveying pipeline 800, one end of which is used to connect to an external aluminum hydroxide conveying device, and the other end of which is connected to the inlet of the third separator 303.

[0089] It is understood that, through the above-described implementation method, aluminum hydroxide in the aluminum hydroxide conveying device can be conveyed to the third separator 303 via the conveying pipeline 800, and then enter the second separator 302 through the solid outlet of the third separator 303 and the inlet of the second separator 302. It is further conveyed to the calcining furnace 200 through the solid outlet and the second inlet of the second separator 302. The aluminum hydroxide will mix with the flue gas in the second separator 302 and the third separator 303. Since the flue gas output from the calcining furnace 200 has a high temperature and has passed through the first separator 301... The flue gas entering the second separator 302 is also at a relatively high temperature. Therefore, aluminum hydroxide will exchange heat with the flue gas inside the second separator 302 and the third separator 303, thereby increasing the temperature of aluminum hydroxide and decreasing the temperature of the flue gas in the second separator 302 and the third separator 303. In this case, aluminum hydroxide can be preheated to reduce subsequent energy consumption and improve the utilization rate of heat in the flue gas. In addition, the decrease in flue gas temperature can also reduce the workload of the spray tower 400 and cooler 503 in subsequent processes.

[0090] The outlet of the spray tower 400 provided in the embodiment of this application is connected to the gas source pipeline 101. The liquefaction component 500 includes a compressor 501. The inlet of the compressor 501 is connected to the outlet of the spray tower 400. The compressor 501 and the gas source pipeline 101 are arranged in parallel.

[0091] It is understood that, through the above-described embodiments, the gaseous product washed by the spray tower 400 can be conveyed to the compressor 501, or the gaseous product washed by the spray tower 400 can be conveyed to the gas source pipeline 101. When the gaseous product is conveyed to the compressor 501, the gaseous product can be compressed to facilitate its collection. When the gaseous product is conveyed to the gas source pipeline 101, the gaseous product can enter the roasting furnace 200 through the gas source pipeline 101, thereby increasing the concentration of the gaseous product in the collection device and reducing the difficulty of subsequent purification.

[0092] It should be noted that the compressor 501 can be a compressor, or a 2-6 stage compression system, or a 3-4 stage compression system. There are no restrictions here, and it can be selected according to the actual use requirements.

[0093] The liquefaction assembly 500 provided in the embodiments of this application further includes: a dehydration component 502 and a cooler 503. The inlet of the dehydration component 502 is connected to the outlet of the compression component 501, the inlet of the cooler 503 is connected to the outlet of the dehydration component 502, and the outlet of the cooler 503 is connected to the inlet of the stripping tower 700.

[0094] Understandably, by setting up the dehydration unit 502, the gaseous products after being cleaned by the spray tower 400 can be dehydrated, and by setting up the cooler 503, the dehydrated gaseous products can be cooled.

[0095] It should be noted that the dehydration component 502 can be an adsorption dehydration device, a gas-liquid separator, a drying tower, an adsorption tower, a membrane separator, or other equipment that can separate gas and liquid. There are no restrictions here, and it can be selected according to the actual use requirements.

[0096] In one embodiment, the dehydration component 502 is an adsorption dehydration device.

[0097] Furthermore, the adsorbent can be one or a combination of activated carbon, molecular sieves, silica gel, activated alumina, or calcium chloride, without limitation, and can be selected according to actual application requirements.

[0098] Understandably, the adsorbent can adsorb water vapor in the gaseous products to dehydrate the gaseous products after they have been cleaned by the 400 spray tower.

[0099] It should be noted that the cooler 503 can be a plate cooler 503, a plate-fin cooler 503, an air cooler, or other equipment that can cool down. There are no restrictions here, and it can be selected according to the actual use requirements.

[0100] The liquefaction assembly 500 provided in the embodiments of this application further includes: an evaporator 504, a distillation column 505, and a throttling valve 506. The evaporator 504 has a first heat exchange pipeline and a second heat exchange pipeline connected by heat conduction. The first heat exchange pipeline is connected to the gas outlet of the first separator 301 and the inlet of the second separator 302, respectively. The distillation column 505 has a column cavity and a fourth inlet, a first outlet, a fifth inlet, and a second outlet, respectively connected to the column cavity. The column cavity is used to contain the cooling medium. Along the height direction of the distillation column 505, the second outlet, The fifth inlet, the fourth inlet, and the first outlet are arranged sequentially at intervals, with the second outlet located at the top of the distillation column 505 and the first outlet located at the bottom of the distillation column 505. The second heat exchange pipeline is connected to the fourth inlet and the first outlet respectively. The cooler 503 has a third heat exchange pipeline and a fourth heat exchange pipeline connected by heat conduction. The third heat exchange pipeline is connected to the outlet of the dehydration unit 502 and the inlet of the stripping column 700 respectively. The fourth heat exchange pipeline is connected to the fifth inlet and the second outlet respectively. The throttle valve 506 is connected between the second outlet and the cooler 503.

[0101] Understandably, through the above implementation method, the cooling medium in the distillation column 505 can flow out through the second outlet and reach the fourth heat exchange pipeline of the cooler 503 after passing through the throttle valve 506. Due to the sudden pressure drop, the cooling medium immediately boils and evaporates violently, absorbing a large amount of latent heat of vaporization, thereby reducing the internal temperature of the fourth heat exchange pipeline. Heat exchange occurs between the fourth and third heat exchange pipelines, resulting in a decrease in the internal temperature of the third heat exchange pipeline, thus cooling the gaseous products in the third heat exchange pipeline. The cooling medium in the fourth heat exchange pipeline can be refluxed back into the distillation column 505 through the fifth inlet, and then guided into the second heat exchange pipeline of the evaporator 504 through the first outlet. Heat exchange occurs between the second and first heat exchange pipelines. The first heat exchange pipeline can serve as a heat source for the second heat exchange pipeline, heating the cooling medium to form a high-temperature, high-pressure gaseous cooling medium. This high-temperature, high-pressure gaseous cooling medium is refluxed back into the distillation column 505 through the fourth inlet, where it condenses and reduces to a normal-temperature, high-pressure liquid cooling medium. During this process, the heat between the first separator 301 and the second separator 302 can be recovered and utilized.

[0102] It should be noted that the cooling medium can be concentrated ammonia, lithium bromide, hydrofluoroolefin, or other media. There are no restrictions, and the appropriate medium can be selected according to the actual usage requirements.

[0103] In one embodiment, the cooling medium is concentrated ammonia.

[0104] Understandably, the concentrated ammonia solution in distillation column 505 can flow out through the second outlet and, after passing through the throttle valve 506, reach the fourth heat exchange line of cooler 503. Due to the sudden pressure drop, the concentrated ammonia solution immediately boils and evaporates violently, forming a gas-liquid mixture of ammonia and absorbing a large amount of latent heat of vaporization. This lowers the internal temperature of the fourth heat exchange line, and heat exchange occurs between the fourth and third heat exchange lines, causing a decrease in the internal temperature of the third heat exchange line. This cools the gaseous products within the third heat exchange line. The gas-liquid mixture of ammonia in the four heat exchange pipelines can be refluxed into the distillation column 505 through the fifth inlet, and then guided into the second heat exchange pipeline of the evaporator 504 through the first outlet. Heat exchange occurs between the second heat exchange pipeline and the first heat exchange pipeline. The first heat exchange pipeline can serve as the heat source for the second heat exchange pipeline to heat the gas-liquid mixture of ammonia and form high-temperature, high-pressure gaseous ammonia vapor. The high-temperature, high-pressure gaseous ammonia vapor is refluxed into the distillation column 505 through the fourth inlet and condensed and reduced to room-temperature, high-pressure liquid ammonia in the distillation column 505.

[0105] The stripping tower 700 provided in the embodiments of this application has a third outlet, a sixth inlet and a seventh inlet connected together. The third outlet is located at the bottom of the stripping tower 700, the sixth inlet is located at the top of the stripping tower 700, and the seventh inlet is connected to the outlet of the cooler 503. The sixth inlet includes a first sub-inlet, a second sub-inlet and a third sub-inlet connected in parallel. The third outlet is used to connect an external carbon dioxide collection device and is connected to the first sub-inlet. The second sub-inlet is connected to the inlet of the dehydration unit 502 and the third sub-inlet is connected to the inlet of the compression unit 501.

[0106] Understandably, the gaseous medium cooled by the cooler 503 can flow into the stripper 700 through the seventh inlet, liquefy into liquid carbon dioxide in the stripper 700, and then be discharged to the carbon dioxide collection device through the third outlet. Alternatively, the liquid carbon dioxide can flow back to the top of the stripper 700 through the third outlet and the first sub-inlet as a refrigerant to cool the gaseous carbon dioxide at the top of the stripper 700. A portion of the non-condensable gas can flow into the dehydration unit 502 through the second sub-inlet, or another portion of the non-condensable gas can flow into the compressor 501 through the third sub-inlet. These two portions of non-condensable gas can re-enter the liquefaction unit 500, reuse the cooling capacity, and be re-captured to improve the carbon dioxide capture rate.

[0107] It should be noted that the non-condensable gas can be nitrogen, carbon dioxide, oxygen, or a mixture of at least two of the above gases, and there are no restrictions on this.

[0108] The collection component 600 provided in the embodiments of this application includes: an output pipeline 601 and a heat exchanger 602, wherein the output pipeline 601 is connected to the outlet of the preheater 102 and the heat exchanger 602 is connected to the output pipeline 601.

[0109] Understandably, the alumina entering the preheater 102 can be discharged to the outside through the output pipeline 601, and the heat exchanger 602 is used to cool the alumina in the output pipeline 601.

[0110] like Figure 2 As shown, an embodiment of this application provides a collection method applied to the collection device provided in any of the above embodiments, comprising the following steps:

[0111] S01: Input the material into the preheating component 100 and preheat it through the preheating component 100;

[0112] S02: The preheated material is conveyed to the roasting furnace 200, where it is burned to generate separation products;

[0113] S03: The separation product is conveyed to the separation component 300, where it is separated into gaseous and solid products.

[0114] S04: The gaseous product is conveyed to the spray tower 400, which is used to clean the gaseous product;

[0115] S05: The cleaned gaseous product is conveyed to the liquefaction component 500. The liquefaction component 500 is used to pressurize and cool the cleaned gaseous product to convert the gaseous product into a liquid product and remove moisture. The separation component 300 is also used to provide a heat source to the liquefaction component 500.

[0116] S06: The cooled gaseous product is transported to the stripping tower 700;

[0117] S07: Convey the solid product to the collection component 600.

[0118] Understandably, by setting up the preheating component 100, the material can be preheated so that the temperature of the material can rise evenly. By setting up the roasting furnace 200, the preheated material can be heated so that the material can be burned in the roasting furnace 200 to generate separation products. The separation products can be conveyed to the separation component 300, where they are separated into gaseous products and solid products. The separated gaseous products can be conveyed to the spray tower 400, cleaned by the spray tower 400, and then conveyed to the liquefaction component 500. The liquefaction component 500 can cool down the cleaned gaseous products. The cooled gaseous products can be conveyed to the stripping tower 700 to capture the gaseous products. The separated solid products can be conveyed to the collection component 600 for collection. By connecting the liquefaction component 500 and the separation component 300 through heat conduction, the separation component 300 can exchange heat with the liquefaction component 500. This allows the separation product in the separation component 300 to be cooled down, while the separation component 300 can also provide a heat source to the liquefaction component 500, thereby cooling down the product to be separated. This reduces the workload of the spray tower 400 and the liquefaction component 500 in subsequent processes and also improves the heat utilization rate of the product to be separated.

[0119] It should be noted that the material is oxygen, and the oxygen concentration is ≥95wt%.

[0120] It is understandable that replacing air with oxygen as a combustion-supporting agent allows the combustion products to be mainly carbon dioxide and water, thereby reducing the volume and content of nitrogen in the flue gas after combustion, thus increasing the carbon dioxide content in the flue gas and making it easier to capture carbon dioxide.

[0121] In one embodiment, the oxygen concentration is ≥98wt%.

[0122] It is understandable that replacing air with oxygen as a combustion-supporting agent allows the combustion products to be mainly carbon dioxide and water, thereby reducing the volume and content of nitrogen in the flue gas after combustion, thus increasing the carbon dioxide content in the flue gas and making it easier to capture carbon dioxide.

[0123] It should be noted that the temperature of the oxygen after preheating is 550℃ to 700℃.

[0124] It is understandable that the above-described implementation method allows the temperature of oxygen to rise evenly.

[0125] In one embodiment, the temperature of the oxygen after preheating is 580°C to 650°C.

[0126] It is understandable that the above-described implementation method allows the temperature of oxygen to rise evenly.

[0127] It should be noted that the internal temperature of the roasting furnace 200 is 850℃ to 1000℃.

[0128] It is understandable that the above-described implementation method allows aluminum hydroxide to undergo a high-temperature decomposition reaction.

[0129] In one embodiment, the internal temperature of the roasting furnace 200 is 900°C to 950°C.

[0130] It is understandable that the above-described implementation method allows aluminum hydroxide to undergo a high-temperature decomposition reaction.

[0131] The collection method provided in the embodiments of this application further includes: conveying aluminum hydroxide to the inlet of the third separator 303, and after preheating by the third separator 303 and the second separator 302, conveying it to the calcining furnace 200.

[0132] It is understood that the above-described embodiments can preheat aluminum hydroxide and improve the heat utilization rate inside the third separator 303 and the second separator 302.

[0133] It should be noted that the temperature of the preheated aluminum hydroxide is between 240℃ and 320℃.

[0134] It is understandable that the above-described implementation method allows the temperature of aluminum hydroxide to rise uniformly.

[0135] In one embodiment, the temperature of the preheated aluminum hydroxide is 260°C to 300°C.

[0136] It is understandable that the above-described implementation method allows the temperature of aluminum hydroxide to rise uniformly.

[0137] The capture method provided in the embodiments of this application further includes: the oxygen content in the gaseous product at the outlet of the spray tower 400 is 10wt% to 30wt%.

[0138] It is understandable that the above-described implementation method can enrich the aluminum hydroxide roasting process with oxygen, thereby allowing carbon dioxide in the flue gas to be enriched.

[0139] In one embodiment, the oxygen content in the gaseous product at the outlet of the spray tower 400 is 12 wt% to 20 wt%.

[0140] It is understandable that the above-described implementation method can enrich the aluminum hydroxide roasting process with oxygen, thereby allowing carbon dioxide in the flue gas to be enriched.

[0141] The collection method provided in the embodiments of this application further includes: cooling the solid product to 40°C to 55°C in the collection component 600.

[0142] It is understandable that the above-described embodiments facilitate the collection of the solid product, alumina.

[0143] The capture method provided in the embodiments of this application further includes: the temperature of the separation component 300 is 900°C to 950°C, and after providing a heat source to the liquefaction component 500, the temperature of the separation component 300 is reduced to 700°C to 850°C.

[0144] It is understandable that the above-described implementation method can improve the utilization rate of heat in the separation component 300.

[0145] In one embodiment, after a heat source is supplied to the liquefaction component 500, the separation component 300 is cooled to 750°C to 800°C.

[0146] It is understandable that the above-described implementation method can improve the utilization rate of heat in the separation component 300.

[0147] The capture method provided in the embodiments of this application further includes reducing the solid content in the gaseous product to below 20 ppm before it is conveyed to the spray tower 400.

[0148] It is understandable that the above implementation method can reduce the load on the spray tower 400 in order to protect the spray tower 400.

[0149] In one embodiment, the solid content in the gaseous product is reduced to below 5 ppm before being conveyed to the spray tower 400.

[0150] It is understandable that the above implementation method can reduce the load on the spray tower 400 in order to protect the spray tower 400.

[0151] The collection method provided in the embodiments of this application further includes: after cleaning by a spray tower 400, the solid content in the gaseous product is reduced to below 1 ppm.

[0152] It is understandable that the above implementation method can provide safety protection for the back-end liquefaction component 500.

[0153] The capture method provided in the embodiments of this application further includes: the purity of the liquid carbon dioxide extracted from the stripping tower 700 is ≥95%.

[0154] It is understandable that the above-described implementation method facilitates the capture of carbon dioxide.

[0155] In one embodiment, the purity of the liquid carbon dioxide extracted by the stripping tower 700 is ≥98%.

[0156] It is understandable that the above-described implementation method facilitates the capture of carbon dioxide.

[0157] The capture method provided in the embodiments of this application further includes: concentrated ammonia water is distilled in a distillation column 505 to obtain high-pressure ammonia gas at the top of the column, with a pressure of 1MPa to 2MPa. After cooling, it is converted into liquid ammonia, and then the pressure is reduced to 0.01MPa to 0.6MPa through a throttling valve 506. At this time, the temperature of the gas-liquid mixed ammonia drops sharply to 0°C to 20°C. The ammonia after heat exchange through a cooler 503 is returned to the distillation column 505 for recycling. The distillate at the bottom of the distillation column 505 is dilute ammonia water with a mass concentration of 3% to 30%.

[0158] It is understandable that the carbon dioxide inside the cooler 503 can be cooled through the above-described implementation method.

[0159] In one embodiment, concentrated ammonia water is distilled in distillation column 505 to obtain high-pressure ammonia gas at the top of the column, with a pressure of 1.3 MPa to 1.8 MPa. Throttling valve 506 reduces the pressure to 0.1 MPa to 0.4 MPa, and the temperature of the gas-liquid mixed ammonia drops sharply to 5°C to 12°C. The distillate at the bottom of distillation column 505 is dilute ammonia water with a mass concentration of 8% to 20%.

[0160] It is understandable that the carbon dioxide inside the cooler 503 can be cooled through the above-described implementation method.

[0161] It should be noted that the terms "one embodiment," "embodiment," "exemplary embodiment," "some embodiments," etc., mentioned in the specification indicate that the described embodiment may include a specific feature, structure, or characteristic, but not every embodiment necessarily includes that specific feature, structure, or characteristic. Furthermore, such phrases do not necessarily refer to the same embodiment. Moreover, when a specific feature, structure, or characteristic is described in connection with an embodiment, implementing such a feature, structure, or characteristic in conjunction with other embodiments, whether explicitly described or not, is within the knowledge scope of those skilled in the art.

[0162] Generally speaking, terms should be understood at least in part by their use in context. For example, at least in part by context, the term "one or more" as used in the text can be used to describe any feature, structure, or characteristic of the singular meaning, or a combination of features, structures, or characteristics of the plural meaning. Similarly, at least in part by context, terms such as "a" or "the" can also be understood to convey either singular or plural usage.

[0163] It should be readily understood that the terms “on,” “above,” and “on top of” in this application should be interpreted in the broadest possible sense, such that “on” means not only “directly on something” but also “on something” with an intermediate feature or layer therebetween, and that “above” or “on top of” means not only “on something” but also “on something” without an intermediate feature or layer therebetween (i.e., directly on something).

[0164] Furthermore, for ease of explanation, spatially relative terms such as "below," "below," "under," "above," and "above" may be used 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 other than those shown in the figures. The device may have other orientations (rotated 90° or in other orientations), and the spatially relative descriptive terms used herein may be interpreted accordingly.

[0165] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A CO2 capture system, characterized in that, include: A preheating assembly (100) includes a gas source line (101) and a preheater (102). The inlet of the gas source line (101) is used to connect to an external oxygen delivery device, and the preheater (102) is connected to the gas source line (101). A roasting furnace (200) has a first inlet, a second inlet and a third inlet connected in series. The first inlet is connected to the outlet of the gas source pipeline (101), and the third inlet is used to connect to external gas. A separation component (300) has its inlet connected to the outlet of the roasting furnace (200); A spray tower (400) has its inlet connected to the outlet of the separation component (300), and its outlet is connected to the gas source pipeline (101). A liquefaction component (500) is provided, the inlet of which is connected to the outlet of the spray tower (400), and the liquefaction component (500) is thermally connected to the separation component (300). A collection component (600) is connected to the separation component (300); A stripping tower (700) is connected to the liquefaction unit (500); The separation component (300) includes: The first separator (301) has its inlet connected to the outlet of the roasting furnace (200), and its solid outlet is connected to the gas source pipeline (101) of the preheating component (100). The second separator (302) has its inlet connected to the gas outlet of the first separator (301), and its solid outlet connected to the second inlet of the roasting furnace (200). The third separator (303) has its inlet connected to the gas outlet of the second separator (302), and its solid outlet is connected to the gas outlet of the first separator (301) and the inlet of the second separator (302), respectively. The liquefaction component (500) includes: A compressor (501) has its inlet connected to the outlet of the spray tower (400); A dehydration component (502) has its inlet connected to the outlet of the compression component (501); Cooler (503), the inlet of which is connected to the outlet of the dehydration unit (502), and the outlet of which is connected to the inlet of the stripping tower (700); Evaporator (504), the evaporator (504) having a first heat exchange pipeline and a second heat exchange pipeline connected by heat conduction, the first heat exchange pipeline being connected to the gas outlet of the first separator (301) and the inlet of the second separator (302) respectively; A distillation column (505) has an inner cavity and a fourth inlet, a first outlet, a fifth inlet, and a second outlet respectively communicating with the inner cavity. The inner cavity is used to contain a cooling medium. Along the height direction of the distillation column (505), the second outlet, the fifth inlet, the fourth inlet, and the first outlet are arranged sequentially at intervals, and the second outlet is located at the top of the distillation column (505), and the first outlet is located at the bottom of the distillation column (505). The second heat exchange pipeline is connected to the fourth inlet and the first outlet, respectively; The cooler (503) has a third heat exchange pipeline and a fourth heat exchange pipeline connected by heat conduction. The third heat exchange pipeline is connected to the outlet of the dehydration unit (502) and the inlet of the stripping tower (700), respectively. The fourth heat exchange pipeline is connected to the fifth inlet and the second outlet, respectively.

2. The CO2 capture system according to claim 1, characterized in that, The separation component (300) also includes; The dust removal component (304) has its inlet connected to the gas outlet of the third separator (303), its gas outlet connected to the inlet of the spray tower (400), and its solid outlet connected to the gas source pipeline (101).

3. The CO2 capture system according to claim 2, characterized in that, Also includes: A conveying pipeline (800) is provided, one end of which is connected to an external aluminum hydroxide conveying device, and the other end of which is connected to the inlet of the third separator (303).

4. The CO2 capture system according to any one of claims 1-3, characterized in that, The compressor (501) and the gas source pipeline (101) are connected in parallel.

5. The CO2 capture system according to claim 4, characterized in that, The liquefaction component (500) further includes: A throttle valve (506) is connected between the second outlet and the cooler (503).

6. The CO2 capture system according to claim 4, characterized in that, The stripping tower (700) has a third outlet, a sixth inlet and a seventh inlet connected together. The third outlet is located at the bottom of the stripping tower (700), the sixth inlet is located at the top of the stripping tower (700), and the seventh inlet is connected to the outlet of the cooler (503). The sixth inlet includes a first sub-inlet, a second sub-inlet, and a third sub-inlet connected in parallel. The third outlet is used to connect to an external carbon dioxide collection device, and the third outlet is connected to the first sub-inlet; The second sub-inlet is connected to the inlet of the dehydration component (502); The third sub-inlet is connected to the inlet of the compression component (501).

7. The CO2 capture system according to any one of claims 1-3, characterized in that, The collection component (600) includes: The output pipeline (601) is connected to the outlet of the preheater (102); A heat exchanger (602) is connected to the output line (601).

8. A CO2 capture method, applied to the CO2 capture system according to any one of claims 1-7, characterized in that, Includes the following steps: The material is fed into the preheating component (100) and preheated by the preheating component (100); The preheated material is conveyed to a roasting furnace (200), where it is burned to generate separation products; The separated product is conveyed to a separation component (300), where it is separated into a gaseous product and a solid product. The gaseous product is conveyed to a spray tower (400) for cleaning the gaseous product; The cleaned gaseous product is conveyed to the liquefaction unit (500), which is used to pressurize and cool the cleaned gaseous product to convert it into a liquid product and remove moisture; wherein, the separation unit (300) is also used to provide a heat source to the liquefaction unit (500). The cooled gaseous product is then transported to a stripping tower (700). Solid products are transported to the collection component (600).

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