Two-stage coupling carbon capture and alkali reduction reaction gas volume control method

Abstract

The application discloses a two-stage coupling carbon fixation and alkali reduction reaction gas volume control method, which comprises the following steps: S1, determining the material quantity of high-alkali substances introduced into each container per unit time; S2, determining the flue gas quantity of the flue gas required to be introduced into each container per unit time according to the material quantity; S3, determining the first threshold range of the flue gas introduced into the first-stage container per unit time and the second threshold range of the flue gas introduced into each second-stage container according to the corresponding flue gas quantity; and S4, if the flow measured by the first flowmeter is located outside the first threshold range, the flow of the first branch pipe is adjusted by adjusting the opening degree of the first valve; and if the flow measured by the second flowmeter is located outside the second threshold range, the flow of the second branch pipe is adjusted by adjusting the opening degree of the second valve. The control method can control the supply quantity of the flue gas in real time, so that the flue gas and the fly ash can be kept in a proper proportion, and the sufficiency of the acid-alkali neutralization reaction is ensured.

Description

Technical Field

[0001] This invention relates to the field of high-alkali solid waste treatment technology, specifically to a two-stage coupled carbon fixation and alkali reduction reaction gas flow control method. Background Technology

[0002] Currently, the main treatment method for high-alkali solid wastes such as fly ash is chemical treatment, which involves neutralizing the flue gas emitted from coal-fired power plants (which contains a large amount of acidic waste gas) with fly ash through an acid-base neutralization reaction. This can simultaneously reduce the alkali metal content of the solid waste and the acidic gases in the waste gas.

[0003] The above reaction process requires a specialized reaction system. Existing reaction systems include reaction vessels, into which both flue gas and fly ash are introduced for acid-base neutralization. However, these systems suffer from low reaction efficiency. Furthermore, the supply of flue gas can be insufficient or excessive, leading to an imbalance in the ratio of flue gas to fly ash and reducing the sufficiency of the acid-base neutralization reaction. Summary of the Invention

[0004] The present invention aims to at least partially solve one of the technical problems in the related art.

[0005] Therefore, this invention proposes a two-stage coupled carbon fixation and alkali reduction reaction gas flow control method. This method can regulate the flue gas supply in real time, thereby ensuring that the flue gas and fly ash maintain a suitable ratio and guaranteeing the sufficiency of the acid-base neutralization reaction.

[0006] The two-stage coupled carbon fixation and alkali reduction reaction gas volume control method of this invention is based on a carbon fixation and alkali reduction system. The carbon fixation and alkali reduction system includes a flue gas pipeline network, a primary container, and multiple secondary containers located downstream of the primary container. The flue gas pipeline network includes a primary main pipe, a first branch pipe, and multiple second branch pipes. The first branch pipe and the multiple second branch pipes are arranged in parallel and are all connected downstream of the primary main pipe. The primary container is connected to the first branch pipe, and the multiple second branch pipes are connected to the multiple second branch pipes in a one-to-one correspondence. The first branch pipe is equipped with a first valve and a first flow meter, and each second branch pipe is equipped with a second valve and a second flow meter.

[0007] The control method includes the following steps:

[0008] S1: Determine the amount of high-alkali material fed into the primary container and each of the secondary containers per unit time;

[0009] S2: Determine the amount of flue gas required to be introduced into the primary container and each of the secondary containers per unit time based on the amount of material.

[0010] S3: Determine the first threshold range of the flue gas introduced into the primary container per unit time and the second threshold range of the flue gas introduced into each secondary container based on the corresponding flue gas volume;

[0011] S4: If the flow rate measured by the first flow meter is outside the first threshold range, the flow rate of the first branch pipe is adjusted by adjusting the opening of the first valve until the flow rate measured by the first flow meter is within the first threshold range.

[0012] If the flow rate measured by the second flow meter is outside the second threshold range, the flow rate of the second branch pipe is adjusted by adjusting the opening of the second valve until the flow rate measured by the second flow meter is within the second threshold range.

[0013] The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method of this invention can regulate the flue gas supply in real time, thereby ensuring that the flue gas and fly ash maintain a suitable ratio and guaranteeing the sufficiency of the acid-base neutralization reaction.

[0014] In some embodiments, the flue gas pipeline network includes a secondary main pipe, the secondary main pipe and the first branch pipe are connected in parallel and are both connected downstream of the primary main pipe, a plurality of second branch pipes are connected in parallel and are all connected downstream of the secondary main pipe, the primary main pipe is provided with a third valve and a third flow meter, and the secondary main pipe is provided with a fourth valve and a fourth flow meter.

[0015] In some embodiments, if the flow rate measured by the third flow meter is outside the third threshold range, the flow rate of the primary main pipe is adjusted by adjusting the opening of the third valve until the flow rate measured by the third flow meter is within the third threshold range.

[0016] If the flow rate measured by the fourth flow meter is outside the fourth threshold range, the flow rate of the secondary main pipe is adjusted by adjusting the opening of the fourth valve until the flow rate measured by the fourth flow meter is within the fourth threshold range.

[0017] In some embodiments, the lower limit of the fourth threshold range is obtained by summing the lower limits of a plurality of second threshold ranges, and the upper limit of the fourth threshold range is obtained by summing the upper limits of a plurality of second threshold ranges.

[0018] The lower limit of the third threshold range is obtained by summing the lower limit of the first threshold range and the lower limit of the fourth threshold range, and the upper limit of the third threshold range is obtained by summing the upper limit of the first threshold range and the upper limit of the fourth threshold range.

[0019] In some embodiments, a fan is included, the fan being disposed at the primary main pipe, the fan being used to pressurize the flue gas and pump the flue gas to the primary container and / or each of the secondary containers.

[0020] In some embodiments, the fan has multiple speed settings, and the number of speed settings of the fan is positively correlated with the total number of the primary container and the plurality of secondary containers connected downstream of the fan.

[0021] In some embodiments, a first pressure gauge, a second pressure gauge, a third pressure gauge, and a fourth pressure gauge are included, wherein the first pressure gauge is located on the first branch pipe, the second pressure gauge is located on the second branch pipe, the third pressure gauge is located on the primary main pipe, and the fourth pressure gauge is located on the secondary main pipe.

[0022] In some embodiments, a slurry pipeline network is included, wherein the primary container and a plurality of the secondary containers are disposed in the slurry pipeline network, and the slurry pipeline network is used to transport the slurry discharged from the primary container to each of the secondary containers.

[0023] In some embodiments, the carbon fixation and alkali reduction system includes a reaction vessel, a flow meter, a first concentration meter, and a second concentration meter. The flow meter and the first concentration meter are located at the inlet of the reaction vessel, and the second concentration meter is located at the outlet of the reaction vessel. The primary vessel or the secondary vessel constitutes the reaction vessel.

[0024] In some embodiments, the carbon fixation and alkali reduction system includes the following steps in use:

[0025] K1: The inlet gas flow rate Q at the inlet of the reaction vessel is measured by the flow meter, and the carbon dioxide concentration at the inlet of the reaction vessel is measured by the first concentration meter. The carbon dioxide concentration at the outlet of the reaction vessel was measured using the second concentration meter. ;

[0026] K2: Determines the intake air flow rate Q and the carbon dioxide concentration within a set time period. The carbon dioxide concentration ;

[0027] K3: Substitute into the following formula to obtain the carbon fixation amount within a set time period. ;

[0028] ...Equation 1

[0029] In Equation 1: Q represents the intake airflow rate within a set time period. This refers to the carbon dioxide concentration at the inlet of the reaction vessel during a set time period. This refers to the carbon dioxide concentration at the outlet of the reaction vessel during a set time period. Attached Figure Description

[0030] Figure 1 This is a schematic diagram of the carbon fixation and alkali reduction system according to an embodiment of the present invention.

[0031] Figure 2 This is a schematic flowchart of the gas volume control method of the present invention.

[0032] Figure 3 This is a schematic diagram of the structure of the reaction vessel in an embodiment of the present invention.

[0033] Figure label:

[0034] 11. Flue gas pipeline network; 12. Primary container; 13. Secondary container; 14. First branch pipe; 15. Secondary branch pipe; 16. Primary main pipe; 17. Secondary main pipe; 18. Third valve; 19. Fan; 110. Third flow meter; 111. First valve; 112. First flow meter; 113. Second valve; 114. Fourth valve; 115. Fourth flow meter; 116. Third pressure gauge; 117. First pressure gauge; 118. Second pressure gauge; 119. Fourth pressure gauge; 120.

[0035] Reaction vessel 21; slurry outlet 211; feed inlet 212; water inlet 213; flow meter 22; first concentration meter 23; second concentration meter 24; air inlet network 25; main pipeline 251; branch pipeline 252; distribution valve 26; first dryer 27; second dryer 28. Detailed Implementation

[0036] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0037] The two-stage coupled carbon sequestration and alkali reduction reaction gas flow control method of this invention requires a carbon sequestration and alkali reduction system for application. This system includes a flue gas pipeline network 11, a primary container 12, and multiple secondary containers 13 located downstream of the primary container 12. For example, ... Figure 1 As shown, there may be only one primary container 12 and two secondary containers 13. Both primary container 12 and secondary container 13 are used to provide space for the reaction of flue gas and fly ash. Liquids such as water need to be added to primary container 12 and secondary container 13 so that flue gas and fly ash are in the form of slurry in primary container 12 or secondary container 13, which can dissolve flue gas and improve the efficiency of acid-base neutralization reaction.

[0038] The carbon fixation and alkali reduction system also includes a slurry pipeline network (not shown). The primary container 12 and each secondary container 13 are located in the slurry pipeline network. During use, the slurry pipeline network is used to transport the slurry in the primary container 12 to the secondary container 13. This can improve the overall efficiency of the acid-base neutralization reaction. On the other hand, the primary container 12 and the secondary container 13 can adopt relatively independent strategies for different stages of the acid-base neutralization reaction, thus targeting different reaction stages and further improving the sufficiency and efficiency of the reaction.

[0039] like Figure 1 As shown, the flue gas pipeline network 11 includes a primary main pipe 16, a first branch pipe 14, and multiple second branch pipes 15. The first branch pipe 14 and the multiple second branch pipes 15 are arranged in parallel and are all connected downstream of the primary main pipe 16. A primary container 12 is connected to the tail end of the first branch pipe 14, and multiple secondary containers 13 are connected one-to-one to the tail ends of the multiple second branch pipes 15. Thus, in use, flue gas can be simultaneously delivered to the primary container 12 and each of the secondary containers 13 via the flue gas pipeline network 11. A first valve 111 and a first flow meter 112 are provided on the first branch pipe 14, and a second valve 114 and a second flow meter 113 are provided on each second branch pipe 15.

[0040] like Figure 2 As shown, the reaction gas volume control method of this embodiment includes the following steps:

[0041] S1: Determine the amount of highly alkaline material fed into the primary container 12 and each secondary container 13 per unit time. For example, highly alkaline materials such as fly ash can be weighed before being poured into the primary container 12 and secondary container 13, and the amount of highly alkaline material can be obtained by calculation. In some other embodiments, the amount of material can also be measured in real time using a device such as a solid flow meter.

[0042] S2: Determine the amount of flue gas required to be introduced into the primary container 12 and each secondary container 13 per unit time based on the amount of material. Specifically, since the amount of fly ash per unit time is determined, the amount of flue gas required for complete acid-base neutralization can be calculated using chemical formulas.

[0043] S3: Determine the first threshold range of flue gas introduced into the primary container 12 per unit time and the second threshold range of flue gas introduced into each secondary container 13 based on the corresponding flue gas volume. Specifically, the amount of high-alkali material in each container (primary container 12 or secondary container 13) can be measured in advance. Thus, the required flue gas volume for each container can be obtained. Due to the influence of factors such as flue gas concentration, fly ash concentration, and conveying rate, the required flue gas volume will change dynamically. Therefore, based on the calculated flue gas volume, a reasonable range of flue gas volume can be given based on experience and numerical simulation. This range is the first threshold range or the second threshold range.

[0044] S4: During the acid-base neutralization reaction, if the flow rate measured by the first flow meter 112 is outside the first threshold range, the flow rate of the first branch pipe 14 is adjusted by adjusting the opening of the first valve 111. Specifically, when the flow rate measured by the first flow meter 112 is higher than the first threshold range, the opening of the first valve 111 can be reduced. When the flow rate measured by the first flow meter 112 is lower than the first threshold range, the opening of the first valve 111 can be increased until the flow rate measured by the first flow meter 112 is within the first threshold range.

[0045] If the flow rate measured by the second flow meter 113 is outside the second threshold range, the flow rate of the second branch pipe 15 is adjusted by adjusting the opening of the second valve 114. Specifically, when the flow rate measured by the second flow meter 113 is higher than the second threshold range, the opening of the second valve 114 can be reduced. When the flow rate measured by the second flow meter 113 is lower than the second threshold range, the opening of the second valve 114 can be increased until the flow rate measured by the second flow meter 113 is within the second threshold range.

[0046] The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method of this invention can regulate the flue gas supply in real time, thereby ensuring that the flue gas and fly ash maintain a suitable ratio and guaranteeing the sufficiency of the acid-base neutralization reaction.

[0047] In some embodiments, such as Figure 1 As shown, the flue gas pipeline network 11 includes a secondary main pipe 17, the secondary main pipe 17 and the first branch pipe 14 are connected in parallel and are all connected downstream of the primary main pipe 16, and multiple second branch pipes 15 are connected in parallel and are all connected downstream of the secondary main pipe 17. The primary main pipe 16 is equipped with a third valve 18 and a third flow meter 110. The total flue gas volume can be directly observed by the third flow meter 110, and the overall opening and closing control of the flue gas pipeline network 11 can be realized by the third valve 18, which facilitates the rapid disconnection of the flue gas pipeline network 11.

[0048] The secondary main pipe 17 is equipped with a fourth valve 115 and a fourth flow meter 116. The fourth flow meter 116 allows for direct observation of the total flue gas volume of the multiple second branch pipes 15, while the fourth valve 115 enables the opening and closing control of the flue gas in all secondary containers 13, thus facilitating the overall control of the primary and secondary acid-base neutralization reactions.

[0049] In some embodiments, if the flow rate measured by the third flow meter 110 is outside the third threshold range, the flow rate of the primary main pipe 16 is adjusted by adjusting the opening of the third valve 18. Specifically, when the flow rate measured by the third flow meter 110 is higher than the third threshold range, the opening of the third valve 18 can be reduced. When the flow rate measured by the third flow meter 110 is lower than the third threshold range, the opening of the third valve 18 can be increased until the flow rate measured by the third flow meter 110 is within the third threshold range.

[0050] If the flow rate measured by the fourth flow meter 116 is outside the fourth threshold range, the flow rate of the secondary main pipe 17 is adjusted by adjusting the opening of the fourth valve 115. Specifically, when the flow rate measured by the fourth flow meter 116 is higher than the fourth threshold range, the opening of the fourth valve 115 can be reduced. When the flow rate measured by the fourth flow meter 116 is lower than the fourth threshold range, the opening of the fourth valve 115 can be increased until the flow rate measured by the fourth flow meter 116 is within the fourth threshold range.

[0051] In some embodiments, the lower limit of the fourth threshold range is obtained by summing the lower limits of a plurality of second threshold ranges, and the upper limit of the fourth threshold range is obtained by summing the upper limits of a plurality of second threshold ranges.

[0052] Specifically, each secondary container 13 has a corresponding second threshold range during use, and each second threshold range has an upper limit and a lower limit. The lower limit of each second threshold range is summed to obtain the lower limit of the fourth threshold range, and the upper limit of each second threshold range is summed to obtain the upper limit of the fourth threshold range. Therefore, the control precision of the secondary main pipe 17 over the flue gas is lower than that of each second branch pipe 15, allowing the secondary main pipe 17 to maintain relative transport stability under normal conditions.

[0053] Optionally, the lower limit of the third threshold range is obtained by summing the lower limits of the first and fourth threshold ranges, and the upper limit of the third threshold range is obtained by summing the upper limits of the first and fourth threshold ranges. This allows the control precision of the primary main pipe 16 over the flue gas to be lower than that of the first branch pipe 14 and the secondary main pipe 17, ensuring that the primary main pipe 16 maintains relative transport stability under normal conditions and avoiding the potential impact of frequent adjustments on the reactions within all containers.

[0054] In some embodiments, the carbon sequestration and alkali reduction system includes a fan 19, which is located in the primary main pipe 16. The fan 19 is used to pressurize the flue gas and pump it to the primary container 12 and / or each secondary container 13. This ensures the pumping pressure within the flue gas pipeline network 11 and guarantees the stability of the pumping.

[0055] In some embodiments, the blower 19 has multiple speed settings, which are positively correlated with the total number of primary containers 12 and multiple secondary containers 13 connected downstream of the blower 19. For example, the blower 19 can be a Roots blower and can have two speed settings: a lower speed setting with lower output power and a higher speed setting with higher output power. When only the primary container 12 is undergoing an acid-base neutralization reaction, the blower 19 can switch to the lower speed setting; when both the primary container 12 and all the secondary containers 13 are undergoing an acid-base neutralization reaction, the blower 19 can switch to the higher speed setting. This allows the output power of the blower 19 to match actual needs, reducing power consumption and achieving energy conservation and emission reduction. Furthermore, when the number of connected containers is small, reducing the power of the blower 19 can enhance the overall structural stability.

[0056] It is understood that in some other embodiments, the fan 19 may also have three, four, five or other speed settings, in which case the number of speed settings of the fan 19 can be adaptively increased or decreased according to the number of connected secondary containers 13.

[0057] In some embodiments, the carbon sequestration and alkali reduction system includes a first pressure gauge 118, a second pressure gauge 119, a third pressure gauge 117, and a fourth pressure gauge 120. The first pressure gauge 118 is located in the first branch pipe 14, the second pressure gauge 119 is located in the second branch pipe 15, the third pressure gauge 117 is located in the primary main pipe 16, and the fourth pressure gauge 120 is located in the secondary main pipe 17. This facilitates direct monitoring of the pressure in the primary main pipe 16, the secondary main pipe 17, the first branch pipe, and each of the second branch pipes.

[0058] In some embodiments, the carbon fixation and alkali reduction system also includes multiple pressure transmitters. Pressure transmitters can be installed on the primary main pipe 16, the first branch pipe, the secondary main pipe 17, and the second branch pipe, thereby further facilitating the control of flue gas pressure.

[0059] In some embodiments, the carbon fixation and alkali reduction system includes a reaction vessel 21, a flow meter 22, a first concentration meter 23, and a second concentration meter 24. The flow meter 22 and the first concentration meter 23 are located at the inlet of the reaction vessel 21, and the second concentration meter 24 is located at the outlet of the reaction vessel 21. A primary container 12 or a secondary container 13 constitutes the reaction vessel 21. Optionally, a flow meter 22 and a first concentration meter 23 may be provided at the inlet of the primary container 12 and each reaction vessel 21, and a second concentration meter 24 may be provided at the outlet of each. In some other embodiments, the flow meter 22, the first concentration meter 23, and the second concentration meter 24 may only be provided in the primary container 12.

[0060] Specifically, such as Figure 3 As shown, the reaction vessel 21 can be a tank, kettle, or similar container. The top of the reaction vessel 21 may be equipped with a feed inlet 212, a water inlet 213, and an exhaust outlet. High-alkali waste materials such as fly ash can be poured into the reaction vessel 21 through the feed inlet 212, while water can be added to the reaction vessel 21 through the water inlet 213, thus providing the necessary environmental conditions for the reaction of fly ash and flue gas. The exhaust outlet allows the gases generated after the acid-base neutralization reaction to be discharged from the reaction vessel 21. The bottom of the reaction vessel 21 may also be equipped with a slurry outlet 211, through which the slurry produced after the reaction can be discharged.

[0061] In this embodiment, both the first concentration meter 23 and the second concentration meter 24 are concentration meters used to measure carbon dioxide concentration, specifically carbon dioxide concentration analyzers. The reaction vessel 21 has a flue gas inlet. The first concentration meter 23 and the flow meter 22 are both located at the inlet of the reaction vessel 21, while the second concentration meter 24 is located at the exhaust port of the reaction vessel 21.

[0062] The carbon fixation and alkali reduction system of this invention may further include the detection of carbon fixation amount during use. Specifically, the method for obtaining the carbon fixation amount may include the following steps:

[0063] K1: The inlet gas flow rate Q at the inlet of reaction vessel 21 is measured by flow meter 22, and the carbon dioxide concentration at the inlet of reaction vessel 21 is measured by first concentration meter 23. The carbon dioxide concentration at the outlet of reaction vessel 21 is measured using a second concentration meter 24. .

[0064] K2: Determines the intake airflow rate Q and carbon dioxide concentration within a set time period. carbon dioxide concentration For example, during an acid-base neutralization reaction in reaction vessel 21, the inlet gas flow rate Q and carbon dioxide concentration can be monitored simultaneously within the same time period (a set time period). carbon dioxide concentration Data collection is performed. It should be noted that the set time period can be a lengthy period, or if the length is short, the set time can be considered a specific point in time.

[0065] K3: After data collection is complete, the three collected data points can be substituted into the following formula to obtain the amount of carbon solidified in reaction vessel 21 due to the acid-base neutralization reaction within the set time period. ;

[0066] ...Equation 1

[0067] In Equation 1: Q represents the intake airflow rate within a set time period. The carbon dioxide concentration at the inlet of reaction vessel 21 is set for a specific time period. The carbon dioxide concentration at the outlet of reaction vessel 21 within a set time period.

[0068] The method for calculating the carbon sequestration and reduction of high-alkali solid waste in this invention embodiment only requires the inlet air flow rate Q and carbon dioxide concentration during measurement. carbon dioxide concentration Data can be collected and then directly substituted into the formula to obtain the corresponding carbon fixation amount. The acquisition process is simple and convenient, avoiding the need for a series of chemical operations in related technologies. This simplifies the process flow, avoids poor detection accuracy due to frequent operational errors, improves the accuracy of the results, and also improves processing efficiency.

[0069] In addition, the carbon fixation amount can be measured at any time during the operation. The whole process has almost no impact on the entire carbon fixation and alkali reduction system, which also ensures the continuity of production and avoids the situation where production is delayed when the measurement is carried out by sampling in related technologies.

[0070] In some embodiments, carbon fixation The calculation process includes the following formulas:

[0071] ...Equation 2

[0072] ...Equation 3

[0073] ...Formula 4

[0074] ...Formula 5

[0075] ...Formula 6

[0076] ...Formula 7

[0077] ...Formula 8

[0078] In equations 2 to 8: Q represents the intake airflow rate within a set time period. The carbon dioxide concentration at the inlet of reaction vessel 21 is set for a specific time period. The carbon dioxide concentration at the outlet of reaction vessel 21 is set for a specific time period. The volume of other gases at the inlet of reaction vessel 21 within a set time period; The volume of carbon dioxide at the inlet of reaction vessel 21 during a set time period; This refers to the volume of carbon dioxide at the outlet of reaction vessel 21 within a set time period.

[0079] In some embodiments, carbon fixation The calculation process includes the following steps:

[0080] A1: Combining equations 5 and 6, we obtain equation 7.

[0081] A2: Substituting equation 7 into equation 4, we get equation 8.

[0082] A3: Substituting equations 3 and 8 into equation 2 and simplifying, we obtain equation 1. For example, substituting equations 3 and 8 into equation 2 yields the following formula:

[0083]

[0084] Then, by simplifying the above formula, we can obtain Formula 1.

[0085] The above refers to carbon sequestration. The calculation process can simplify and cancel out some irrelevant parameters, making the final result simpler and avoiding the situation in related technologies where many parameters need to be measured to obtain the carbon fixation amount.

[0086] In some embodiments, the carbon fixation and alkali reduction system includes an air inlet network 25, which includes a main pipeline 251 and a plurality of branch pipelines 252. The inlets of the plurality of branch pipelines 252 are all connected to the outlets of the main pipeline 251, and the outlets of the plurality of branch pipelines 252 are all connected to the reaction vessel 21. At least some of the outlets of the branch pipelines 252 are arranged at intervals in the height direction and / or circumferential direction of the reaction vessel 21. A flow meter 22 is provided on the main pipeline 251.

[0087] For example, such as Figure 3As shown, the intake duct network 25 can be considered as part of the flue gas duct network 11. The intake duct network 25 may include a main duct 251 and two branch ducts 252. In some other embodiments, the number of branch ducts 252 may also be three, four, five, etc. The inlets of the two branch ducts 252 are connected to the outlets of the main duct 251, and the outlets of the two branch ducts 252 are connected to the reaction vessel 21. The outlets of the two branch ducts 252 are arranged at intervals both vertically and circumferentially in the reaction vessel 21. For example, the outlet of one branch duct 252 may be located at the front upper part of the reaction vessel 21, and the outlet of the other branch duct 252 may be located at the rear lower part of the reaction vessel 21.

[0088] The flow meter 22 is installed on the main pipeline 251, so that all the flue gas flowing into the reaction vessel 21 through the inlet pipeline 25 can pass through the flow meter 22, ensuring the accuracy of the measurement.

[0089] In use, the intake pipe network 25 is used to transport the flue gas generated by the coal-fired power plant. The flue gas can enter different positions of the reaction vessel 21 through multiple branch pipes 252, thereby ensuring the uniformity of the distribution of the flue gas in the reaction vessel 21, which in turn helps to ensure the sufficiency of the acid-base neutralization reaction.

[0090] In some embodiments, such as Figure 3 As shown, the intake pipe network 25 includes a distribution valve 26, which is located between the main pipe 251 and multiple branch pipes 252. The distribution valve 26 is used to control the on / off state and flow rate regulation of the main pipe 251 and each branch pipe 252. This facilitates the control of the on / off state and flow rate of the main pipe 251 and branch pipes 252.

[0091] In some embodiments, the dispensing valve 26 includes the following steps in use:

[0092] B1: If the amount of carbon fixation obtained If the carbon fixation amount is less than the set threshold, the carbon fixation amount can be obtained through the above steps. Since the specific composition of fly ash and flue gas will change under actual working conditions, the carbon fixation amount can be considered as a full reaction within a certain range. The set threshold can be the lower limit of the carbon fixation amount when the flue gas and fly ash have a full acid-base neutralization reaction. When it is lower than this value, there may be an excessive amount of flue gas entering the system. At this time, the flow area of ​​at least part of the branch pipe 252 can be reduced by controlling the distribution valve 26, thereby reducing the amount of flue gas entering the system.

[0093] B2: The above methods and steps can be used again to adjust the carbon fixation content. Calculations are performed to obtain the carbon sequestration amount. If the flow rate remains below the set threshold, the control valve 26 will continue to reduce the flow area of ​​at least a portion of the branch pipe 252 or close a portion of the branch pipe 252. This further reduces the flue gas flow rate, thereby ensuring a proper ratio between the flue gas and the slurry in the reaction vessel 21, thus guaranteeing a complete reaction.

[0094] In some embodiments, a reflux line (not shown) is connected between the reaction vessel 21 and the main pipeline 251, depending on the amount of carbon solidification obtained. If the gas level is below a set threshold, the return pipeline is connected so that the gas discharged through the reaction vessel 21 can flow back into the reaction vessel. This allows the discharged gas to flow back into the reaction vessel 21 via the inlet pipeline 25, and the acid-base neutralization reaction can be carried out again within the reaction vessel 21, further ensuring the sufficiency of the reaction, guaranteeing the amount of carbon fixation, and preventing the discharged gas from exceeding the pollutant limits.

[0095] In some embodiments, such as Figure 3 As shown, the first concentration meter 23 is connected to the main pipe 251 and located between the flow meter 22 and the connection between the main pipe 251 and multiple branch pipes 252. A first dryer 27 is provided between the first concentration meter 23 and the main pipe 251. The first dryer 27 can dry the gas flowing into the first concentration meter 23, thereby preventing water vapor and other substances from entering the first concentration meter 23. This improves the accuracy of carbon dioxide measurement and prevents water vapor and other substances from damaging the concentration meter.

[0096] In some embodiments, such as Figure 3 As shown, the second concentration meter 24 is installed on top of the reaction vessel 21, and a second dryer 28 is provided between the second concentration meter 24 and the reaction vessel 21. This prevents water vapor and other substances from entering the second concentration meter 24 and ensures the accuracy of the measurement results from the second concentration meter 24.

[0097] In some embodiments, at least a portion of the cross-sectional area of ​​the reaction vessel 21 gradually decreases from bottom to top, for example, as shown in the figure. Figure 3 As shown, the reaction vessel 21 is generally conical in shape, with multiple branch pipes 252 outlets arranged at intervals along the vertical direction, and the distance between the outlets of two adjacent branch pipes 252 gradually decreasing from bottom to top. This ensures that the distribution of the branch pipes 252 outlets roughly corresponds to the volume distribution of the slurry within the reaction vessel 21, thereby further guaranteeing the uniformity of flue gas distribution within the reaction vessel 21.

[0098] In some embodiments, the carbon fixation and alkali reduction system includes a stirring device (not shown), which is disposed inside the reaction vessel 21, and when the amount of carbon fixation obtained... When the value is below a set threshold (which can be calculated using the method described above), the stirring speed of the agitator is increased. Since the reaction between the flue gas and slurry may be incomplete due to uneven distribution during the reaction process, increasing the stirring speed of the agitator allows for more uniform mixing of the flue gas and slurry, ensuring the adequacy of the acid-base neutralization reaction and thus increasing the carbon fixation rate.

[0099] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0100] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0101] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0102] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0103] In this invention, the terms "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to a specific feature, structure, material, or characteristic described in connection with that embodiment or example, which is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0104] Although the above embodiments have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Any changes, modifications, substitutions and variations made to the above embodiments by those skilled in the art are within the protection scope of the present invention.

Claims

1. A method for controlling the gas flow rate of a two-stage coupled carbon fixation and alkali reduction reaction, characterized in that, Based on the carbon sequestration and alkali reduction system, the carbon sequestration and alkali reduction system includes a flue gas pipeline network, a primary container, and multiple secondary containers located downstream of the primary container. The flue gas pipeline network includes a primary main pipe, a first branch pipe, and multiple second branch pipes. The first branch pipe and multiple second branch pipes are arranged in parallel and are all connected downstream of the primary main pipe. The primary container is connected to the first branch pipe, and the multiple secondary containers are connected to the multiple second branch pipes one by one. The first branch pipe is equipped with a first valve and a first flow meter, and each second branch pipe is equipped with a second valve and a second flow meter. The control method includes the following steps: S1: Determine the amount of high-alkali material fed into the primary container and each of the secondary containers per unit time; S2: Determine the amount of flue gas required to be introduced into the primary container and each of the secondary containers per unit time based on the amount of material. S3: Determine the first threshold range of the flue gas introduced into the primary container per unit time and the second threshold range of the flue gas introduced into each secondary container based on the corresponding flue gas volume; S4: If the flow rate measured by the first flow meter is outside the first threshold range, the flow rate of the first branch pipe is adjusted by adjusting the opening of the first valve until the flow rate measured by the first flow meter is within the first threshold range. If the flow rate measured by the second flow meter is outside the second threshold range, the flow rate of the second branch pipe is adjusted by adjusting the opening of the second valve until the flow rate measured by the second flow meter is within the second threshold range.

2. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 1, characterized in that, The flue gas pipeline network includes a secondary main pipe, which is connected in parallel with the first branch pipe and is also connected downstream of the primary main pipe. Multiple second branch pipes are connected in parallel and are also connected downstream of the secondary main pipe. The primary main pipe is equipped with a third valve and a third flow meter, and the secondary main pipe is equipped with a fourth valve and a fourth flow meter.

3. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 2, characterized in that, If the flow rate measured by the third flow meter is outside the third threshold range, the flow rate of the primary main pipe is adjusted by adjusting the opening of the third valve until the flow rate measured by the third flow meter is within the third threshold range. If the flow rate measured by the fourth flow meter is outside the fourth threshold range, the flow rate of the secondary main pipe is adjusted by adjusting the opening of the fourth valve until the flow rate measured by the fourth flow meter is within the fourth threshold range.

4. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 3, characterized in that, The lower limit of the fourth threshold range is obtained by summing the lower limits of multiple second threshold ranges, and the upper limit of the fourth threshold range is obtained by summing the upper limits of multiple second threshold ranges. The lower limit of the third threshold range is obtained by summing the lower limit of the first threshold range and the lower limit of the fourth threshold range, and the upper limit of the third threshold range is obtained by summing the upper limit of the first threshold range and the upper limit of the fourth threshold range.

5. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 2, characterized in that, Includes a fan located in the primary main pipe, the fan being used to pressurize the flue gas and pump the flue gas to the primary container and / or each of the secondary containers.

6. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 5, characterized in that, The fan has multiple speed settings, and the number of the fan speed settings is positively correlated with the total number of the primary container and the multiple secondary containers connected downstream of the fan.

7. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 2, characterized in that, It includes a first pressure gauge, a second pressure gauge, a third pressure gauge and a fourth pressure gauge. The first pressure gauge is located on the first branch pipe, the second pressure gauge is located on the second branch pipe, the third pressure gauge is located on the primary main pipe, and the fourth pressure gauge is located on the secondary main pipe.

8. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 1, characterized in that, The system includes a slurry pipeline network, in which the primary container and multiple secondary containers are located, and the slurry pipeline network is used to transport the slurry discharged from the primary container to each of the secondary containers.

9. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to any one of claims 1-8, characterized in that, The carbon fixation and alkali reduction system includes a reaction vessel, a flow meter, a first concentration meter, and a second concentration meter. The flow meter and the first concentration meter are located at the inlet of the reaction vessel, and the second concentration meter is located at the outlet of the reaction vessel. The primary vessel or the secondary vessel constitutes the reaction vessel.

10. The two-stage coupled carbon fixation and alkali reduction reaction gas flow control method according to claim 9, characterized in that, The carbon fixation and alkali reduction system includes the following steps in use: K1: The inlet gas flow rate Q at the inlet of the reaction vessel is measured by the flow meter, and the carbon dioxide concentration at the inlet of the reaction vessel is measured by the first concentration meter. The carbon dioxide concentration at the outlet of the reaction vessel was measured using the second concentration meter. ; K2: Determines the intake air flow rate Q and the carbon dioxide concentration within a set time period. The carbon dioxide concentration ; K3: Substitute into the following formula to obtain the carbon fixation amount within a set time period. ; ...Equation 1 In Equation 1: Q represents the intake airflow rate within a set time period. This refers to the carbon dioxide concentration at the inlet of the reaction vessel during a set time period. This refers to the carbon dioxide concentration at the outlet of the reaction vessel during a set time period.

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