Fly ash carbon fixation and alkali reduction circulation system

Abstract

The application discloses a fly ash carbon fixation and alkali reduction circulating system. The system comprises a primary container, multiple secondary containers, a slurry pipe network, a flue gas pipe network, a backflow pipe network and an exhaust pipe network. The multiple secondary containers are arranged in parallel, and the volume sum of the multiple secondary containers is not less than the volume of the primary container. The primary container and the multiple secondary containers are connected to the slurry pipe network, and the multiple secondary containers are located downstream of the primary container. The primary container and the multiple secondary containers are connected to the flue gas pipe network. The backflow pipe network is connected between the primary container and the multiple secondary containers. The gas discharged from each secondary container can be discharged back to the primary container through the backflow pipe network. One end of the exhaust pipe network is connected to the primary container, and the other end of the exhaust pipe network is used for being connected to a flue gas pipe of a coal-fired power plant. The system can ensure sufficient reaction of flue gas, avoid the situation that the content of carbon dioxide in the treated tail gas is still high, ensure the treatment effect, and improve the treatment efficiency.

Description

Technical Field

[0001] This invention relates to the field of high-alkali solid waste treatment technology, specifically to a fly ash carbon sequestration and alkali reduction recycling system. Background Technology

[0002] Currently, the main treatment method for high-alkali solid wastes such as fly ash is chemical treatment. This involves neutralizing the flue gas emitted from coal-fired power plants (which contains a significant amount of acidic waste gas) with fly ash through an acid-base reaction. This simultaneously reduces the alkali metal content of the solid waste and the acidic gases in the waste gas. However, the systems used for carbon sequestration and alkali reduction of fly ash suffer from problems such as incomplete reaction, persistently high carbon dioxide content in the treated exhaust gas, and low overall treatment efficiency. Summary of the Invention

[0003] The present invention aims to at least partially solve one of the technical problems in the related art.

[0004] Therefore, this invention proposes a fly ash carbon fixation and alkali reduction circulation system. This system can ensure the full reaction of flue gas, avoid the situation where the treated tail gas still has a high carbon dioxide content, ensure the treatment effect, and improve the treatment efficiency.

[0005] The fly ash carbon sequestration and alkali reduction recycling system of this invention includes:

[0006] The system comprises a primary container and multiple secondary containers, both of which are used for acid-base neutralization reactions between fly ash and flue gas. The multiple secondary containers are arranged in parallel, and the sum of the volumes of the multiple secondary containers is not less than the volume of the primary container.

[0007] A slurry pipeline network is provided, wherein the primary container and a plurality of secondary containers are connected to the slurry pipeline network, and the plurality of secondary containers are located downstream of the primary container so that the slurry in the primary container can be transported to each of the secondary containers via the slurry pipeline network.

[0008] A flue gas pipeline network, wherein the primary container and the plurality of secondary containers are all connected to the flue gas pipeline network, and the flue gas pipeline network is used to transport flue gas to the primary container and the plurality of secondary containers;

[0009] A return pipeline network is provided, which connects the primary container and the multiple secondary containers, allowing gas discharged from each secondary container to be returned to the primary container via the return pipeline network.

[0010] An exhaust pipe network, one end of which is connected to the primary container, and the other end of which is connected to the flue gas pipeline of a coal-fired power plant, is used to transport the gas discharged from the primary container into the flue gas pipeline and discharge it through the flue gas pipeline.

[0011] The fly ash carbon fixation and alkali reduction circulation system of this invention can ensure the full reaction of flue gas, avoid the situation that the treated tail gas still has a high carbon dioxide content, ensure the treatment effect, and improve the treatment efficiency.

[0012] In some embodiments, the use includes the following steps:

[0013] M1: Fly ash and water are transported to the primary container, and then flue gas is introduced into the primary container through the flue gas pipeline network;

[0014] M2: After the fly ash and flue gas have reacted for a first time, the slurry in the primary container is discharged into multiple secondary containers until the slurry in the primary container is completely discharged.

[0015] M3: Fly ash, water and flue gas are fed into the primary container again and reacted. At the same time, flue gas is introduced into each of the secondary containers through the flue gas pipeline network until the slurry reacts in each of the secondary containers for a second time. Then the slurry in each of the secondary containers is discharged.

[0016] M4: After the slurry in each of the secondary containers has been completely discharged, repeat steps M2 and M3 above until the acid-base neutralization reaction of all fly ash and flue gas is completed.

[0017] In some embodiments, the flue gas pipeline network includes a primary main pipe, a secondary main pipe, a first branch pipe, and a plurality of second branch pipes. The first branch pipe and the secondary main pipe are arranged in parallel and are both connected downstream of the primary main pipe. The plurality of second branch pipes are arranged in parallel and are all connected downstream of the secondary main pipe. The primary container is connected to the tail end of the first branch pipe, and the plurality of secondary containers are connected one-to-one to the tail ends of the plurality of second branch pipes.

[0018] In some embodiments, a first fan, a second fan, and a third fan are included. The first fan is located in the primary main pipe and is used to pressurize the flue gas to deliver the flue gas to the primary container and each of the secondary containers. The second fan is located in the return pipe network and is used to pump the gas discharged from each of the secondary containers to the primary container. The third fan is located in the exhaust pipe network and is used to pump the gas discharged from the primary container to the flue gas duct.

[0019] In some embodiments, the first branch pipe is provided with a first valve and a first flow meter, each second branch pipe is provided with a second valve and a second flow meter, 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.

[0020] In some embodiments, the use includes the following steps:

[0021] S1: Determine the amount of high-alkali material fed into the primary container and each of the secondary containers per unit time;

[0022] 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.

[0023] 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;

[0024] 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.

[0025] 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.

[0026] 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.

[0027] 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.

[0028] 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.

[0029] 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.

[0030] In some embodiments, the connection point between the flue gas duct network and the primary container is lower than the connection point between the return duct network and the primary container, and the connection point between the flue gas duct network and each of the secondary containers is lower than the connection point between the return duct network and each of the secondary containers.

[0031] In some embodiments, the 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.

[0032] In some embodiments, the use includes the following steps:

[0033] 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. ;

[0034] K2: Determines the intake air flow rate Q and the carbon dioxide concentration within a set time period. The carbon dioxide concentration ;

[0035] K3: Substitute into the following formula to obtain the carbon fixation amount within a set time period. ;

[0036] ...Equation 1

[0037] 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

[0038] Figure 1 This is a schematic diagram of the overall structure of the fly ash carbon fixation and alkali reduction circulation system according to an embodiment of the present invention.

[0039] Figure 2 yes Figure 1 A schematic diagram of the flue gas pipeline network.

[0040] Figure 3 yes Figure 1 A partial schematic diagram of a reaction vessel.

[0041] Figure label:

[0042] 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. First 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.

[0043] 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;

[0044] Return pipe network 31; Second air fan 311;

[0045] Exhaust pipe network 41; Third fan 411. Detailed Implementation

[0046] 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.

[0047] like Figure 1 As shown, the fly ash carbon sequestration and alkali reduction circulation system of this embodiment includes a primary container 12, multiple secondary containers 13, a slurry pipeline network, a flue gas pipeline network 11, a return pipeline network 31, and an exhaust pipeline network 41.

[0048] Both the primary container 12 and the secondary container 13 are used for acid-base neutralization reactions between fly ash and flue gas, and multiple secondary containers 13 are arranged in parallel. For example, Figure 1 and Figure 2 As shown, there may be only one primary container 12, and two secondary containers 13. In some other embodiments, there may also be three, four, five, or other types of secondary containers 13.

[0049] Both the primary container 12 and the 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 the primary container 12 and the secondary container 13 so that the flue gas and fly ash are in the form of slurry in the primary container 12 or the secondary container 13, which can dissolve the flue gas and improve the efficiency of acid-base neutralization reaction.

[0050] The sum of the volumes of the multiple secondary containers 13 is not less than the volume of the primary container 12. Therefore, the slurry in the primary container 12 can be completely discharged into the secondary container 13 after a period of reaction, thus meeting the storage capacity requirements of the secondary container 13.

[0051] The primary container 12 and multiple secondary containers 13 are all connected to a slurry pipeline network (not shown), and the multiple secondary containers 13 are all located downstream of the primary container 12 so that the slurry in the primary container 12 can be transported to each secondary container 13 via the slurry pipeline network. This improves the overall efficiency of the acid-base neutralization reaction. Furthermore, the primary container 12 and the secondary containers 13 can employ relatively independent strategies for different stages of the acid-base neutralization reaction, thus targeting different reaction stages effectively and further enhancing the sufficiency and efficiency of the reaction.

[0052] Primary container 12 and multiple secondary containers 13 are all connected to flue gas duct network 11, which is used to transport flue gas into primary container 12 and multiple secondary containers 13. For example, Figure 1 As shown, the inlet end of the flue gas pipeline 11 can be connected to the exhaust pipe of the electric field. The flue gas pipeline 11 has multiple outlet ends, and the primary container 12 and each of the secondary containers 13 can be connected to the multiple outlet ends of the flue gas pipeline 11 respectively. The flue gas generated by the coal-fired power plant can be transported to the primary container 12 or each of the secondary containers 13 through the flue gas pipeline 11.

[0053] The return pipeline 31 connects the primary container 12 and multiple secondary containers 13, allowing gas discharged from each secondary container 13 to be returned to the primary container 12 via the return pipeline 31. Figure 1 As shown, the reflux network 31 can have multiple inlet ends and one outlet end. The multiple inlet ends of the reflux network 31 can be connected to multiple secondary containers 13 respectively, and the outlet end of the reflux network 31 can be connected to the primary container 12.

[0054] In use, the gas discharged from multiple secondary containers 13 can be collected through the return pipe network 31, and then the collected gas can be discharged back into the primary container 12. Thus, the gas discharged from the secondary container 13 can undergo acid-base neutralization reaction again in the primary container 12, thereby ensuring the sufficiency of the reaction and avoiding the situation where the carbon dioxide content of the discharged gas is too high.

[0055] like Figure 1 As shown, one end of the exhaust pipe network 41 is connected to the primary container 12, and the other end of the exhaust pipe network 41 is used to connect to the flue gas pipeline of the coal-fired power plant. The exhaust pipe network 41 is used to transport the gas discharged from the primary container 12 into the flue gas pipeline and then discharge it through the flue gas pipeline. Through the return of the gas, the exhaust gas can also be harmlessly treated by the treatment equipment of the coal-fired power plant itself, thereby further purifying the exhaust gas and avoiding environmental pollution.

[0056] In the fly ash carbon fixation and alkali reduction circulation system of this invention, the gas discharged from each secondary container 13 can be discharged into the primary container 12 and undergo acid-base neutralization reaction again, thereby ensuring the sufficiency of flue gas reaction and avoiding the situation where the treated tail gas still has a high carbon dioxide content, thus ensuring the treatment effect.

[0057] Secondly, in the fly ash carbon fixation and alkali reduction recycling system of this invention, the first stage of the acid-base neutralization reaction can be carried out in the first-stage container 12, and the second stage of the reaction can be carried out in the second-stage container 13, so that the reactions of different processes can be carried out simultaneously and cross-processed, thereby improving the processing efficiency.

[0058] In some embodiments, the fly ash carbon sequestration and alkali reduction circulation system includes the following steps during use:

[0059] M1: Fly ash and water can be transported to the primary container 12 first, and then flue gas can be introduced into the primary container 12 through the flue gas pipeline 11. The fly ash and flue gas can then undergo an acid-base neutralization reaction in the primary container 12.

[0060] M2: After the first reaction time of fly ash and flue gas, the slurry in the primary container 12 is discharged into multiple secondary containers 13 until the slurry in the primary container 12 is completely discharged. For example, after the fly ash and flue gas in the primary container 12 have reacted for 30 minutes, the valve of the slurry pipeline network can be opened, and the slurry in the primary container 12 can be discharged into each of the secondary containers 13 through the slurry pipeline network. It should be noted that the number of secondary containers 13 connected can be determined according to the amount of slurry in the primary container 12. For example, when the amount of slurry is small, fewer secondary containers 13 can be connected, and when the amount of slurry is large, more secondary containers 13 can be connected.

[0061] M3: After the slurry in the primary container 12 is completely drained, fly ash, water, and flue gas are introduced into the primary container 12 again for reaction. Simultaneously, flue gas is introduced into each secondary container 13 through the flue gas pipeline 11 until the slurry reacts in each secondary container 13 for a second time. Then, the slurry in each secondary container 13 is drained. It should be noted that the second time can be equal to or longer than the first time, thus ensuring the completeness of the reaction.

[0062] M4: After the slurry in each secondary container 13 has been completely discharged, repeat steps M2 and M3 above until the acid-base neutralization reaction of all fly ash and flue gas is completed.

[0063] In the above process, the primary container 12 and each secondary container 13 operate synchronously in time, so that different stages of the acid-base neutralization reaction can be carried out simultaneously, improving the reaction efficiency and ensuring the sufficiency of the reaction.

[0064] In some embodiments, since the overall volume of the secondary container 13 is large, some of the secondary containers 13 can also serve as backups. For example, the second duration of the secondary container 13 is longer than the first duration of the primary container 12. The slurry in the primary container 12, which reacts for the first duration, can be discharged into the idle secondary container 13. This allows for the alternating use of some secondary containers 13 and other secondary containers 13, which helps to compensate for the difference in reaction time between the primary container 12 and each of the secondary containers 13, and further improves the reaction efficiency.

[0065] In some embodiments, such as Figure 2 As shown, the flue gas pipeline network 11 includes a primary main pipe 16, a secondary main pipe 17, a first branch pipe 14, and multiple second branch pipes 15. The first branch pipe 14 and the secondary main pipe 17 are arranged in parallel and are both connected to the downstream of the primary main pipe 16. The multiple second branch pipes 15 are arranged in parallel and are all connected to the downstream of the secondary main pipe 17. The primary container 12 is connected to the tail end of the first branch pipe 14, and the multiple secondary containers 13 are connected to the tail ends of the multiple second branch pipes 15 in a corresponding manner.

[0066] In some embodiments, such as Figure 1 As shown, the fly ash carbon fixation and alkali reduction circulation system includes a first fan 19, a second fan 311, and a third fan 411. The first fan 19 is located in the primary main pipe 16 and is used to pressurize the flue gas to deliver it to the primary container 12 and each secondary container 13. The second fan 311 is located in the return pipe network 31 and is used to pump the gas discharged from each secondary container 13 to the primary container 12. The third fan 411 is located in the exhaust pipe network 41 and is used to pump the gas discharged from the primary container 12 to the flue gas pipeline.

[0067] The first fan 19, the second fan 311 and the third fan 411 respectively ensure the transmission pressure in the corresponding pipeline network, and ensure the power and stability of the transmission.

[0068] In some embodiments, the first 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 first blower 19. For example, the first blower 19 can be a Roots blower and can have two speed settings, which can be a low speed setting with lower output power and a high speed setting with higher output power. When only the primary container 12 is undergoing an acid-base neutralization reaction, the first blower 19 can switch to the low speed setting; when both the primary container 12 and all the secondary containers 13 are undergoing an acid-base neutralization reaction, the first blower 19 can switch to the high speed setting.

[0069] Therefore, on the one hand, the output power of the first fan 19 can be matched with the actual needs, which is conducive to reducing power consumption and achieving energy conservation and emission reduction. On the other hand, when the number of containers connected is small, the power of the first fan 19 can also be reduced to enhance the overall structural stability.

[0070] It is understood that in some other embodiments, the first fan 19 may also have three, four, five or other speed settings, in which case the number of speed settings of the first fan 19 can be adaptively increased or decreased according to the number of connected secondary containers 13.

[0071] In some embodiments, such as Figure 2 As shown, the fly ash carbon sequestration and alkali reduction circulation 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.

[0072] In some embodiments, a first valve 111 and a first flow meter 112 are provided on the first branch pipe 14, a second valve 114 and a second flow meter 113 are provided on each second branch pipe 15, a third valve 18 and a third flow meter 110 are provided on the primary main pipe 16, and a fourth valve 115 and a fourth flow meter 116 are provided on the secondary main pipe 17.

[0073] In some embodiments, the fly ash carbon sequestration and alkali reduction circulation system includes the following steps in use:

[0074] 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.

[0075] 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.

[0076] 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.

[0077] 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.

[0078] 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.

[0079] 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.

[0080] 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.

[0081] 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.

[0082] 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.

[0083] 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.

[0084] In some embodiments, such as Figure 1 As shown, the connection between the flue gas pipeline 11 and the primary container 12 is lower than the connection between the return pipeline 31 and the primary container 12. Since the concentration of carbon dioxide in the flue gas in the flue gas pipeline 11 is relatively high, this arrangement is based on the change in carbon dioxide concentration, which allows the high-concentration carbon dioxide flue gas to react for a longer time, further ensuring the sufficiency of the reaction.

[0085] Optionally, the connection points between the flue gas duct network 11 and each secondary container 13 are lower than the connection points between the return duct network 31 and each secondary container 13. This extends the dwell time of the flue gas within the secondary container 13 and facilitates the discharge of the gas after the reaction in the secondary container 13.

[0086] In some embodiments, the fly ash carbon fixation and alkali reduction circulation 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 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. The primary container 12 or the secondary container 13 constitutes the reaction vessel 21.

[0087] 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 container 21, and a second concentration meter 24 may be provided at the outlet. In some other embodiments, the flow meter 22, the first concentration meter 23 and the second concentration meter 24 may be provided only in the primary container 12.

[0088] 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.

[0089] 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.

[0090] In some embodiments, the fly ash carbon sequestration and alkali reduction circulation system may further include the detection of carbon sequestration amount during use. Specifically, the method for obtaining the carbon sequestration amount may include the following steps:

[0091] 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. .

[0092] 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.

[0093] 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. ;

[0094] ...Equation 1

[0095] 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.

[0096] 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.

[0097] 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 fly ash carbon fixation and alkali reduction cycle system, which also ensures the continuity of production and avoids the situation of production delay when measuring by sampling in related technologies.

[0098] In some embodiments, carbon fixation The calculation process includes the following formulas:

[0099] ...Equation 2

[0100] ...Equation 3

[0101] ...Formula 4

[0102] ...Formula 5

[0103] ...Formula 6

[0104] ...Formula 7

[0105] ...Formula 8

[0106] 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.

[0107] In some embodiments, carbon fixation The calculation process includes the following steps:

[0108] A1: Combining equations 5 and 6, we obtain equation 7.

[0109] A2: Substituting equation 7 into equation 4, we get equation 8.

[0110] 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:

[0111]

[0112] Then, by simplifying the above formula, we can obtain Formula 1.

[0113] 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.

[0114] In some embodiments, the fly ash carbon fixation and alkali reduction circulation system includes an air inlet network 25, which includes a main pipeline 251 and multiple branch pipelines 252. The inlets of the multiple branch pipelines 252 are all connected to the outlets of the main pipeline 251, and the outlets of the multiple 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 installed on the main pipeline 251.

[0115] 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.

[0116] 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.

[0117] 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.

[0118] 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.

[0119] In some embodiments, the dispensing valve 26 includes the following steps in use:

[0120] 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.

[0121] 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 is still below the set threshold, the control valve 26 will continue to reduce the flow area of ​​at least part of the branch pipe 252 or close part of the branch pipe 252. This can further reduce the amount of flue gas introduced, thereby making the ratio of flue gas to slurry in the reaction vessel 21 more suitable, thus ensuring the sufficiency of the reaction.

[0122] 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.

[0123] 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.

[0124] 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.

[0125] 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.

[0126] In some embodiments, the fly ash carbon fixation and alkali reduction circulation system includes a stirring device (not shown), which is located inside the reaction vessel 21, and when the obtained carbon fixation amount 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.

[0127] 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.

[0128] 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.

[0129] 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.

[0130] 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.

[0131] 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.

[0132] 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 fly ash carbon sequestration and alkali reduction recycling system, characterized in that, include: The system comprises a primary container and multiple secondary containers, both of which are used for acid-base neutralization reactions between fly ash and flue gas. The multiple secondary containers are arranged in parallel, and the sum of the volumes of the multiple secondary containers is not less than the volume of the primary container. A slurry pipeline network is provided, wherein the primary container and a plurality of secondary containers are connected to the slurry pipeline network, and the plurality of secondary containers are located downstream of the primary container so that the slurry in the primary container can be transported to each of the secondary containers via the slurry pipeline network. A flue gas pipeline network, wherein the primary container and the plurality of secondary containers are all connected to the flue gas pipeline network, and the flue gas pipeline network is used to transport flue gas to the primary container and the plurality of secondary containers; A return pipeline network is provided, which connects the primary container and the multiple secondary containers, allowing gas discharged from each secondary container to be returned to the primary container via the return pipeline network. An exhaust pipe network, one end of which is connected to the primary container, and the other end of which is used to connect to the flue gas pipeline of a coal-fired power plant. The exhaust pipe network is used to transport the gas discharged from the primary container to the flue gas pipeline and discharge it through the flue gas pipeline. The reaction vessel includes 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. The following steps are included in its 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.

2. The fly ash carbon sequestration and alkali reduction recycling system according to claim 1, characterized in that, The following steps are included when using it: M1: Fly ash and water are transported to the primary container, and then flue gas is introduced into the primary container through the flue gas pipeline network; M2: After the fly ash and flue gas have reacted for a first time, the slurry in the primary container is discharged into multiple secondary containers until the slurry in the primary container is completely discharged. M3: Fly ash, water and flue gas are fed into the primary container again and reacted. At the same time, flue gas is introduced into each of the secondary containers through the flue gas pipeline network until the slurry reacts in each of the secondary containers for a second time. Then the slurry in each of the secondary containers is discharged. M4: After the slurry in each of the secondary containers has been completely discharged, repeat steps M2 and M3 above until the acid-base neutralization reaction of all fly ash and flue gas is completed.

3. The fly ash carbon sequestration and alkali reduction recycling system according to claim 1, characterized in that, The flue gas pipeline network includes a primary main pipe, a secondary main pipe, a first branch pipe, and multiple second branch pipes. The first branch pipe and the secondary main pipe are arranged in parallel and are both connected downstream of the primary main pipe. The multiple second branch pipes are arranged in parallel and are all connected downstream of the secondary main pipe. The primary container is connected to the tail end of the first branch pipe, and the multiple secondary containers are connected one-to-one to the tail ends of the multiple second branch pipes.

4. The fly ash carbon sequestration and alkali reduction recycling system according to claim 3, characterized in that, It includes a first fan, a second fan, and a third fan. The first fan is located in the primary main pipe and is used to pressurize the flue gas to deliver the flue gas to the primary container and each of the secondary containers. The second fan is located in the return pipe network and is used to pump the gas discharged from each of the secondary containers to the primary container. The third fan is located in the exhaust pipe network and is used to pump the gas discharged from the primary container to the flue gas pipe.

5. The fly ash carbon sequestration and alkali reduction recycling system according to claim 3, characterized in that, The first branch pipe is equipped with a first valve and a first flow meter, each second branch pipe is equipped with a second valve and a second flow meter, 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.

6. The fly ash carbon sequestration and alkali reduction recycling system according to claim 5, characterized in that, The following steps are included in its use: 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. 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.

7. The fly ash carbon sequestration and alkali reduction recycling system according to claim 6, 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.

8. The fly ash carbon sequestration and alkali reduction recycling system according to claim 1, characterized in that, The connection point between the flue gas duct network and the primary container is lower than the connection point between the return duct network and the primary container, and the connection point between the flue gas duct network and each of the secondary containers is lower than the connection point between the return duct network and each of the secondary containers.

Images