Carbon trapping and sealing system in clinker calcining process
By using a phase change absorber capture tower and regeneration module system during clinker calcination, the problem of carbon dioxide pollution is solved, efficient carbon dioxide capture and storage is achieved, and high-purity carbon dioxide gas is obtained.
Patent Information
- Application Number
- CN202510197237.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-02-21
- Publication Date
- 2025-04-08
AI Technical Summary
The carbon dioxide generated during clinker calcination pollutes the environment. The existing treatment methods such as solution absorption method and physical adsorption method have problems such as complex structure, low efficiency and failure of absorbents at high temperatures.
The phase change absorber is used as a carrier to capture and regenerate carbon dioxide through a circulation loop composed of a capture tower and regeneration module to achieve the acquisition of high-purity carbon dioxide gas.
It realizes efficient capture and storage of carbon dioxide, and directly obtains high-purity carbon dioxide gas, avoids environmental pollution, and simplifies the structure of the treatment system.
Smart Images
Figure CN119771120A_ABST
Abstract
Description
Technical Field
[0001] The present application relates to the field of capture and storage technology, and in particular to a carbon capture and storage system during clinker calcination. Background Art
[0002] The clinker calcination process produces carbon dioxide. In this process, calcium carbonate in the raw material and a small amount of magnesium carbonate mixed in it decompose at high temperature to release carbon dioxide. The specific chemical reaction equation is:
[0003] Magnesium carbonate decomposition: MgCO3→MgO+CO2;
[0004] Calcium carbonate decomposition: CaCO3→CaO+CO2;
[0005] Both reactions are strongly endothermic, and the decomposition temperature is related to the partial pressure of carbon dioxide and the degree of mineral crystallization. In an environment with normal pressure and a decomposed carbon dioxide partial pressure of 1 atmosphere, the decomposition temperature of pure carbonate is 890°C. Therefore, during the clinker calcination process, as the temperature rises, the carbonate in the raw material gradually decomposes, generating a large amount of carbon dioxide emissions.
[0006] Carbon dioxide pollutes the environment. With the continuous improvement of environmental protection requirements, requirements for the carbon dioxide content of waste gas generated during the calcination process have begun to be set. The general treatment process of waste gas generated during the calcination process includes heat recovery treatment and dust removal treatment, and then carbon dioxide recovery treatment.
[0007] The main treatment methods at present are solution absorption and physical adsorption. The solution absorption method uses water, methanol and propylene carbonate as absorbents, and also requires supporting temperature adjustment and pressure adjustment equipment. The overall structure is relatively complex. The molecular sieves used in the physical adsorption method also face the problems of large size and low treatment efficiency. In particular, high temperature will cause potential absorbent failure. Summary of the invention
[0008] The present application provides a carbon capture and storage system during clinker calcination, which uses a phase change absorbent as a carrier to treat the tail gas generated during the clinker calcination process. The phase change absorbent in this way is recycled to directly obtain high-purity carbon dioxide gas.
[0009] The above-mentioned purpose of the present application is achieved through the following technical solutions:
[0010] The present application provides a carbon capture and storage system during clinker calcination, comprising:
[0011] Capture tower and regeneration module;
[0012] A plurality of reaction pipes are arrayed inside the capture tower, and the reaction pipes are divided into two groups;
[0013] An input pipeline, a first end of which is located outside the capture tower and a second end of which extends deep into a corresponding reaction pipeline inside the capture tower;
[0014] Among them, two groups of reaction pipelines work alternately;
[0015] The capture tower and the regeneration module form a circulation loop. The solid matter generated in the capture tower is sent to the regeneration module for decomposition, the decomposed liquid is sent back to the capture tower, and the decomposed gas is sent to the gas storage module.
[0016] In a possible implementation of the present application, it further includes a reaction separation hole cover arranged at intervals in the reaction pipe, and a gap exists between the edge of the reaction separation hole cover and the inner wall of the reaction pipe.
[0017] In a possible implementation of the present application, in a direction close to the input pipe, the width of the gap between the edge of the reaction separation hole cover and the inner wall of the reaction pipe tends to increase.
[0018] In a possible implementation of the present application, baffles are symmetrically arranged in the reaction pipe in a direction close to the input pipe;
[0019] The partition includes two straight edges and two curved edges;
[0020] There are channels between the two straight edges of the partition and the inner wall of the reaction pipe, and the two arc edges of the partition are fixedly connected to the inner wall of the reaction pipe.
[0021] In a possible implementation of the present application, one of the straight edges of the partition is inclined toward a direction close to the input pipe.
[0022] In a possible implementation of the present application, a liquid circulation module forming a loop with the capture tower is also included, and the liquid circulation module is used to drive the liquid in the reaction pipeline to continuously flow;
[0023] The flow direction of the liquid in the reaction pipe is opposite to the flow direction of the gas in the reaction pipe.
[0024] In a possible implementation of the present application, the regeneration module includes:
[0025] Regeneration tower, the internal space is divided into air intake chamber, exhaust chamber and heat exchange chamber;
[0026] A heat exchange pipeline, a first end of which is connected to the air inlet bin;
[0027] The two ends of the return pipe are respectively connected to the exhaust bin and the second end of the heat exchange pipe;
[0028] The distributor is installed inside the regeneration tower.
[0029] In a possible implementation of the present application, the distributor includes:
[0030] A first material distribution disc is fixed inside the regeneration tower;
[0031] A second material distribution disc, rotatably connected to the first material distribution disc;
[0032] A driver, which is arranged on the regeneration tower and connected to the second material distribution disc, and is used to drive the second material distribution disc to reciprocate;
[0033] A rotating arm is provided on the regeneration tower, and is used to push the solid matter on the second distribution plate evenly;
[0034] Wherein, channels are arranged on the first distribution tray and the second distribution tray.
[0035] In a possible implementation of the present application, a liquid level sensor is provided in the heat exchange chamber, and the liquid level sensor is configured to detect the height of the liquid level in the heat exchange chamber. BRIEF DESCRIPTION OF THE DRAWINGS
[0036] Figure 1 It is a structural schematic diagram of a capture and storage system provided in this application.
[0037] Figure 2 This is a schematic diagram of the time distribution of the inflation process and the reaction process in a reaction pipeline provided by the present application.
[0038] Figure 3 It is a schematic diagram of the internal structure of a reaction pipeline provided in this application.
[0039] Figure 4 It is a schematic diagram of the internal structure of a regeneration module provided in this application.
[0040] Figure 5 It is a structural schematic diagram of a distributor provided in this application.
[0041] Figure 6 This is a schematic diagram of the distribution of channels on a first distribution tray provided in the present application.
[0042] In the figure, 1. capture tower, 2. regeneration module, 3. liquid circulation module, 11. reaction pipe, 12. input pipe, 13. reaction separation hole cover, 14. partition, 21. regeneration tower, 22. heat exchange pipe, 23. reflux pipe, 24. distributor, 211. air inlet bin, 212. exhaust bin, 213. heat exchange bin, 214. liquid level sensor, 241. first distribution tray, 242. second distribution tray, 243. drive, 244. rotating arm, 245. channel. DETAILED DESCRIPTION
[0043] The technical solution in this application is further described in detail below in conjunction with the accompanying drawings.
[0044] This application discloses a carbon capture and storage system during clinker calcination. Figure 1 In some examples, the carbon capture and storage system during the clinker calcination process disclosed in the present application includes a capture tower 1, a regeneration module 2, a reaction pipeline 11 and an input pipeline 12.
[0045] The reaction pipes 11 are divided into two groups. The two groups of reaction pipes 11 are arranged in an array inside the capture tower 1. The first end of the input pipe 12 is located outside the capture tower 1, and the second end goes deep into the corresponding reaction pipe 11 inside the capture tower 1.
[0046] The specific implementation method of the alternating operation of the two groups of reaction pipes 11 can be that the number of input pipes 12 is two, and the two input pipes 12 work alternately. A nozzle is installed on the part of the input pipe 12 located in the capture tower 1, and the nozzle extends into the corresponding reaction pipe 11 to inject gas into the reaction pipe 11.
[0047] The two groups of reaction pipes 11 work alternately, that is, in terms of time dimension, the reaction pipes 11 have a charging process and a reaction process. Figure 2 As shown, the aeration process and the reaction process are alternately arranged in time and temperature. The aeration process refers to injecting the tail gas generated during the clinker calcination process into the reaction pipe 11, and the reaction process refers to the reaction of the tail gas injected into the reaction pipe 11 with the phase change absorbent inside the reaction pipe 11.
[0048] The capture tower 1 and the regeneration module 2 form a circulation loop, the solid matter generated in the capture tower 1 is sent to the regeneration module 2 for decomposition, the decomposed liquid is sent back to the capture tower 1, and the decomposed gas is sent to the gas storage module.
[0049] Phase change absorbent is a new type of chemical absorbent, which is mainly used to capture acidic gases in industrial waste gas. The working principle is that after absorbing the acidic gas, the absorbent will spontaneously or through temperature adjustment to separate into a gas-enriched phase. The solid-liquid phase change absorbent used in this application is 1,3-bis(3-aminopropyl)tetramethyldisiloxane silicon liquid-solid phase change absorbent, triethylenetetramine (TETA) + ethanol liquid-solid phase change absorbent or the same type of absorbent.
[0050] When this solid-liquid phase change absorbent absorbs the exhaust gas generated during the clinker calcination process, solid matter will be produced. The solid matter will be sent to the regeneration module 2 for decomposition, and the decomposed liquid, that is, the solid-liquid phase change absorbent, will be returned to the capture tower 1 for use again. The decomposed gas, that is, carbon dioxide, will be stored after being pressurized, and then reused, such as participating in industrial production or power generation or centralized storage.
[0051] The function of the reaction pipe 11 is to provide an independent vertical space. The solid matter generated inside the independent vertical space can fall along the reaction pipe 11 to the bottom of the capture tower 1 and then be sent to the regeneration module 2 for regeneration.
[0052] The purpose of alternating the two groups of reaction pipes 11 is to avoid the continuous disturbance of the solid-liquid phase change absorbent inside the reaction pipes 11 caused by the continuous injection of gas, which leads to a decrease in the solid matter generation rate. Alternating use can also screen the generated solid matter to a certain extent, so that a small volume of solid matter stays in the reaction pipes 11 and grows until the particle size meets the requirements.
[0053] For some examples, see Figure 3 A plurality of reaction separation holes 13 are arranged at intervals inside the reaction pipe 11. There is a gap between the edge of the reaction separation holes 13 and the inner wall of the reaction pipe 11. The functions of the reaction separation holes 13 are as follows:
[0054] Prolonging the residence time of the gas inside the reaction pipe 11;
[0055] The large-volume bubbles are broken to increase the contact area between the bubbles and the solid-liquid phase change absorbent.
[0056] The generated solids slide down to the bottom of the capture tower 1 through the gap between the edge of the reaction separation hole cover 13 and the inner wall of the reaction pipe 11. The specific structure of the reaction separation hole cover 13 is high in the middle and low around, so that the generated solids will not be retained on the reaction separation hole cover 13.
[0057] Furthermore, in the direction close to the input pipe 12, the width of the gap between the edge of the reaction separation hole cover 13 and the inner wall of the reaction pipe 11 tends to increase, in order to prevent the generated solid matter from clogging the gap between the edge of the reaction separation hole cover 13 and the inner wall of the reaction pipe 11.
[0058] In some examples, in the direction close to the input pipe 12, partitions 14 are spaced and symmetrically arranged in the reaction pipe 11, and the partitions 14 include two straight edges and two arc edges. Furthermore, there are channels between the two straight edges of the partition 14 and the inner wall of the reaction pipe 11, and the two arc edges of the partition 14 are fixedly connected to the inner wall of the reaction pipe 11.
[0059] The function of the partition 14 is to further prolong the residence time of the gas inside the reaction pipe 11 and to improve the absorption rate of the solid-liquid phase change absorbent to carbon dioxide.
[0060] In some possible implementations, one of the straight edges of the partition 14 is inclined toward the direction close to the input pipe 12 , in order to prevent solid matter from being retained on the partition 14 .
[0061] For some examples, see Figure 1 A liquid circulation module 3 is added to form a loop with the capture tower 1. The liquid circulation module 3 is used to drive the liquid in the reaction pipe 11 to flow continuously. In terms of the flow direction, the flow direction of the liquid in the reaction pipe 11 is required to be opposite to the flow direction of the gas in the reaction pipe 11.
[0062] This flow mode can increase the residence time of the gas in the reaction pipe 11 to a certain extent, and can also push the generated solid matter to move to the bottom of the capture tower 1, avoiding the solid matter from staying in the reaction pipe 11 for too long and causing the volume to be too large.
[0063] In some examples, the liquid circulation module 3 includes a storage bin and a circulation pump, and the capture tower 1, the storage bin and the circulation pump form a loop.
[0064] For some examples, see Figure 4 The regeneration module 2 includes a distributor 24 , a regeneration tower 21 , a heat exchange pipe 22 , a reflux pipe 23 and a distributor 24 . The space inside the regeneration tower 21 is divided into an air intake bin 211 , an exhaust bin 212 and a heat exchange bin 213 .
[0065] The first end of the heat exchange pipe 22 is connected to the air inlet bin 211 , and the second end is connected to the reflux pipe 23 . The two ends of the reflux pipe 23 are respectively connected to the exhaust bin 212 and the second end of the heat exchange pipe 22 . The distributor 24 is located inside the regeneration tower 21 .
[0066] The air inlet bin 211 is connected to an external hot air source, in which the exhaust gas from the clinker calcination process that has undergone a heat recovery is generally used. The exhaust gas from the clinker calcination process that has undergone a heat recovery enters the air inlet bin 211, and then sequentially passes through the heat exchange pipe 22 and the flow pipe 23 before entering the exhaust bin 212. The exhaust bin 212 is connected to the input pipe 12.
[0067] That is, the tail gas of the clinker calcining process that has undergone secondary heat recovery treatment will enter the capture tower 1 for treatment. When the amount of tail gas of the clinker calcining process that has undergone secondary heat recovery treatment is insufficient, a small amount of tail gas of the clinker calcining process that has undergone primary heat recovery will be introduced into the capture tower 1.
[0068] See also Figure 5 and Figure 6 The distributor 24 includes a first distribution disc 241, a second distribution disc 242, a driver 243 and a rotating arm 244. The first distribution disc 241 is fixed inside the regeneration tower 21, and the second distribution disc 242 is rotatably connected to the first distribution disc 241. The driver 243 is fixedly mounted on the regeneration tower 21 and connected to the second distribution disc 242. The function of the driver 243 is to drive the second distribution disc 242 to rotate reciprocatingly.
[0069] The first distribution tray 241 and the second distribution tray 242 are both provided with a channel 245. During the reciprocating rotation of the second distribution tray 242, the channel 245 on the first distribution tray 241 and the second distribution tray 242 has two states: open and closed.
[0070] When the channel 245 is opened, the solid matter in the first distribution tray 241 and the second distribution tray 242 falls into the heat exchange bin 213. The heat exchange bin 213 includes solid-liquid phase change absorbent and solid matter. The heat exchange pipe 22 and the reflux pipe 23 heat the solid-liquid phase change absorbent to decompose the solid matter in the solid-liquid phase change absorbent. The decomposition temperature is generally controlled at 90°-100°.
[0071] The rotating arm 244 is installed on the regeneration tower 21, and uses a motor as a power source, and its function is to push the solid matter on the second distribution tray 242 evenly. This is because the solid matter generated in the capture tower 1 needs to be sent to the regeneration module 2 through an auger. If the solid matter is transported in this way, the solid matter will be unevenly distributed on the first distribution tray 241 and the second distribution tray 242.
[0072] Uneven distribution will cause the solid matter to be unable to be evenly spread into the heat exchange bin 213 . If the solid matter is unevenly distributed in the heat exchange bin 213 , it will cause uneven temperature distribution in the heat exchange bin 213 , which will directly affect the decomposition process of the solid matter in the heat exchange bin 213 .
[0073] Furthermore, a liquid level sensor 214 is added in the heat exchange chamber 213 , and the liquid level sensor 214 is configured to detect the liquid level in the heat exchange chamber 213 . It is required that the liquid level in the heat exchange chamber 213 always submerges the heat exchange pipe 22 and the reflux pipe 23 .
[0074] When the liquid level in the heat exchange chamber 213 is low, the outflow rate of the solid-liquid phase change absorbent in the heat exchange chamber 213 is reduced, or an appropriate amount of solid-liquid phase change absorbent is directly added.
[0075] The embodiments of this specific implementation method are all preferred embodiments of the present application, and are not intended to limit the protection scope of the present application. Therefore, all equivalent changes made based on the structure, shape, and principle of the present application should be included in the protection scope of the present application.
Claims
1. A carbon capture and storage system during clinker calcination, characterized in that: include: A capture tower (1) and a regeneration module (2); A plurality of reaction pipes (11) are arranged in an array inside the capture tower (1), and the reaction pipes (11) are divided into two groups; An input pipeline (12), a first end of which is located outside the capture tower (1) and a second end of which extends into a corresponding reaction pipeline (11) inside the capture tower (1); Wherein, two groups of reaction pipes (11) work alternately; The capture tower (1) and the regeneration module (2) form a circulation loop, the solid matter generated in the capture tower (1) is sent to the regeneration module (2) for decomposition, the decomposed liquid is sent back to the capture tower (1), and the decomposed gas is sent to the gas storage module.
2. The carbon capture and storage system during clinker calcination according to claim 1, characterized in that: It also includes a reaction separation hole cover (13) arranged at intervals in the reaction pipe (11), and a gap exists between the edge of the reaction separation hole cover (13) and the inner wall of the reaction pipe (11).
3. The carbon capture and storage system during clinker calcination according to claim 2, characterized in that: In the direction approaching the input pipe (12), the width of the gap between the edge of the reaction separation hole cover (13) and the inner wall of the reaction pipe (11) tends to increase.
4. The carbon capture and storage system during clinker calcination according to claim 1, characterized in that: In a direction close to the input pipe (12), partitions (14) are symmetrically arranged in intervals in the reaction pipe (11); The partition (14) comprises two straight edges and two arc-shaped edges; There are channels between the two straight edges of the partition (14) and the inner wall of the reaction pipe (11), and the two arc-shaped edges of the partition (14) are fixedly connected to the inner wall of the reaction pipe (11).
5. The carbon capture and storage system during clinker calcination according to claim 4, characterized in that: One of the straight edges of the partition (14) is inclined toward the direction approaching the input pipe (12).
6. The carbon capture and storage system during clinker calcination according to claim 1, characterized in that: It also includes a liquid circulation module (3) forming a loop with the capture tower (1), and the liquid circulation module (3) is used to drive the liquid in the reaction pipeline (11) to continuously flow; The flow direction of the liquid in the reaction pipe (11) is opposite to the flow direction of the gas in the reaction pipe (11).
7. The carbon capture and storage system during clinker calcination according to claim 1, characterized in that: The regeneration module (2) comprises: The regeneration tower (21) has an internal space divided into an air intake chamber (211), an exhaust chamber (212) and a heat exchange chamber (213); A heat exchange pipe (22), a first end of which is connected to the air inlet bin (211); A reflux pipe (23), both ends of which are respectively connected to the exhaust bin (212) and the second end of the heat exchange pipe (22); The distributor (24) is arranged inside the regeneration tower (21).
8. The carbon capture and storage system during clinker calcination according to claim 7, characterized in that: The distributor (24) comprises: A first material distribution plate (241) is fixed inside the regeneration tower (21); A second material distribution disc (242) is rotatably connected to the first material distribution disc (241); A driver (243) is disposed on the regeneration tower (21) and connected to the second material distribution disk (242), and the driver (243) is used to drive the second material distribution disk (242) to reciprocate; A rotating arm (244) is provided on the regeneration tower (21), and the rotating arm (244) is used to push the solid matter on the second distribution plate (242) evenly; Wherein, the first distribution tray (241) and the second distribution tray (242) are both provided with a channel (245).
9. The carbon capture and storage system during clinker calcination according to claim 7, characterized in that: A liquid level sensor (214) is provided in the heat exchange chamber (213), and the liquid level sensor (214) is configured to detect the height of the liquid level in the heat exchange chamber (213).