Carbon resourceization and collaborative treatment system for coal-fired power plant

Abstract

The application discloses a coal-fired power plant carbon resourceization collaborative treatment system, which comprises a flue gas shunting and desulfurization unit, a carbon dioxide capture and conversion unit, an ammonia recovery unit and a fly ash mineralization unit; the flue gas shunting and desulfurization unit comprises a desulfurization tower; the carbon dioxide capture and conversion unit comprises a cooling tower and a decarbonization tower connected in sequence, and the cooling tower is connected with the desulfurization tower; the ammonia recovery unit is connected with the decarbonization tower to input liquid ammonia into the decarbonization tower; the fly ash mineralization unit comprises a solid leaching reactor and a continuous mineralization reactor connected with the solid leaching reactor, and the continuous mineralization reactor is connected with the desulfurization tower. The coal-fired power plant carbon resourceization collaborative treatment system can be applied to large-scale resourceization recovery of carbon dioxide and fly ash, has low process energy consumption, can realize synchronous high-value conversion of CO2 and fly ash, and reduces environmental pollution and resource waste.

Description

Technical Field

[0001] This application relates to the fields of power generation and resource recycling technology, specifically to the field of carbon sequestration and co-processing of solid waste in coal-fired power plants, and particularly to a carbon resource recovery co-processing system for coal-fired power plants. Background Technology

[0002] With the increasing emissions of greenhouse gases, represented by carbon dioxide (CO2), global ecosystems are under serious threat, and effectively addressing the CO2 emission problem has become a focus of widespread attention for researchers. In recent years, numerous demonstration and commercial projects of carbon dioxide capture, utilization, and storage (CCUS) have been carried out globally. However, due to high production costs and immature operating models, most projects have not been successful. The flue gas from coal-fired power plants is characterized by large volumes, low concentrations (only about 12%), and complex compositions, posing significant challenges to the application of CCUS technology in coal-fired power plants.

[0003] Fly ash is a major solid waste generated after coal combustion in coal-fired power plants. Its resource utilization faces significant challenges: on the one hand, existing utilization pathways are limited and of limited value (mainly used as a raw material for building materials, with generally low added value); on the other hand, the problem of massive stockpiling is prominent, and some stockpiles are located in environmentally sensitive areas, posing environmental and safety risks such as dust pollution, heavy metal leaching, and land occupation. It is worth noting that fly ash has a large specific surface area and is rich in alkali metals and alkaline earth metal compounds such as CaO, which provides a potential technical pathway for its adsorption and fixation of CO2 through carbonation reactions. Utility Model Content

[0004] Therefore, it is necessary to provide a coal-fired power plant carbon resource synergistic treatment system that can achieve simultaneous high-value conversion of CO2 and fly ash, reducing environmental pollution and resource waste.

[0005] One embodiment of this application provides a collaborative processing system for carbon resource utilization in coal-fired power plants.

[0006] A coal-fired power plant carbon resource recovery and co-processing system includes a flue gas diversion and desulfurization unit, a carbon dioxide capture and conversion unit, an ammonia recovery unit, and a fly ash mineralization unit.

[0007] The flue gas diversion and desulfurization unit includes a desulfurization tower, which is used to absorb and oxidize the raw flue gas from the coal-fired power plant to form desulfurized flue gas and generate crude ammonium sulfate product.

[0008] The carbon dioxide capture and conversion unit includes a cooling tower and a decarbonization tower connected in sequence. The cooling tower is connected to the desulfurization tower to cool a portion of the desulfurized flue gas from the desulfurization tower, and the decarbonization tower is used to decarbonize the cooled desulfurized flue gas.

[0009] The ammonia recovery unit is connected to the decarbonization tower so that liquid ammonia is fed into the decarbonization tower to react with carbon dioxide in the decarbonization tower to produce crude ammonium bicarbonate.

[0010] The fly ash mineralization unit includes a solid leaching reactor and a continuous mineralization reactor connected to the solid leaching reactor. The solid leaching reactor is used to receive fly ash discharged from a coal-fired power plant and, after leaching and filtration with a circulating medium, obtain Ca-containing fly ash. 2+ The solution, the continuous mineralization reactor connected to the desulfurization tower, utilizes the solution containing Ca. 2+ The mineralizing solution reacts with a portion of the desulfurized flue gas from the desulfurization tower to produce crude calcium carbonate.

[0011] In some embodiments, the ammonia recovery unit includes a liquid ammonia reactor connected to the decarbonization tower, wherein the liquid ammonia reactor generates liquid ammonia by adding urea and feeds it into the decarbonization tower to react with carbon dioxide in the decarbonization tower to generate crude ammonium bicarbonate.

[0012] In some embodiments, the ammonia recovery unit further includes a urea storage tank connected to the liquid ammonia reactor for introducing urea into the liquid ammonia reactor;

[0013] In some embodiments, a drive pump is installed on the pipeline between the urea storage tank and the liquid ammonia reactor.

[0014] In some embodiments, a control valve is installed on the pipeline between the urea storage tank and the liquid ammonia reactor.

[0015] In some embodiments, a flow detection device is installed on the pipeline between the urea storage tank and the liquid ammonia reactor.

[0016] In some embodiments, the ammonia recovery unit further includes an ammonium bicarbonate storage tank connected to the decarbonization tower to store the crude ammonium bicarbonate.

[0017] In some embodiments, the ammonia recovery unit further includes a centrifuge connected between the ammonium bicarbonate storage tank and the decarbonization tower, the centrifuge being used to centrifuge and thicken the crude ammonium bicarbonate.

[0018] In some embodiments, the ammonia recovery unit further includes a two-stage ammonia washing tower connected to the decarbonization tower. The two-stage ammonia washing tower absorbs the escaped ammonia in the decarbonization tower by adding desulfurization absorbent for secondary use, and discharges the washed flue gas.

[0019] In some embodiments, the two-stage ammonia washing tower is also connected to the desulfurization tower to recycle the absorbed liquid ammonia back to the desulfurization tower for reuse.

[0020] In some embodiments, the coal-fired power plant carbon resource utilization co-processing system further includes an ammonium sulfate post-processing unit connected to the desulfurization tower. The ammonium sulfate post-processing unit is used to post-process the crude ammonium sulfate product generated from the desulfurization tower after it has been concentrated and crystallized by the heat of the raw flue gas from the coal-fired power plant.

[0021] In some embodiments, the fly ash mineralization unit further includes a mineralization liquid reactor connected between the solid leaching reactor and the continuous mineralization reactor. The mineralization liquid reactor is activated by adding ammonia, a directing agent, and the Ca-containing... 2+ The solutions are mixed and the pH is adjusted to form the mineralizing solution used for the mineralization reaction.

[0022] The aforementioned coal-fired power plant carbon resource recovery and co-processing system is applicable to large-scale resource recovery of carbon dioxide and fly ash. It features low energy consumption and enables simultaneous high-value conversion of CO2 and fly ash, reducing environmental pollution and resource waste. Specifically, the core of this application lies in the cooling and diversion of desulfurized flue gas. Part of the desulfurized flue gas enters a cooling tower for cooling treatment before entering a decarbonization tower, while the other part enters a continuous mineralization reactor. This achieves simultaneous delivery of desulfurized flue gas to both the decarbonization tower and the continuous mineralization reactor, allowing for direct treatment of low-concentration CO2 (e.g., CO2 concentration of 12%~15%) without enrichment. In the first branch, the desulfurized flue gas reacts with liquid ammonia to achieve a carbon capture rate of ≥75%, producing agricultural-grade ammonium bicarbonate with a nitrogen content of ≥17%. In the second branch, the desulfurized flue gas contacts a fly ash-based mineralization liquid in a counter-current manner, simultaneously fixing ≥0.2 t / t of fly ash, producing building-grade lightweight calcium carbonate with a purity >90%.

[0023] Furthermore, the aforementioned coal-fired power plant carbon resource utilization and co-processing system achieves the recycling of liquid ammonia through an ammonia circulation mechanism. The two-stage ammonia washing tower absorbs the escaped ammonia in the decarbonization tower by adding desulfurization absorbent liquid for secondary utilization and discharges the washed flue gas. The recovery rate of the two-stage ammonia washing tower is >95%, which can be closed-loop with calcium leaching-mineralization reaction. The recycling medium reuse rate is >80%, which significantly reduces operating costs.

[0024] In summary, compared with traditional technologies, this application has at least the following beneficial effects:

[0025] (1) Dual-path synergistic carbon capture mechanism: This application sets up a decarbonization tower and a continuous mineralization reactor. The flue gas from the coal-fired power plant is absorbed and oxidized in the desulfurization tower to form desulfurized flue gas and generate crude ammonium sulfate product. Part of the desulfurized flue gas enters the cooling tower for cooling treatment and then enters the decarbonization tower. Part of the desulfurized flue gas enters the continuous mineralization reactor, realizing the simultaneous delivery of desulfurized flue gas to the decarbonization tower and the continuous mineralization reactor. On the one hand, the decarbonization tower decarbonizes the cooled desulfurized flue gas and inputs liquid ammonia into the decarbonization tower to react with carbon dioxide in the decarbonization tower to generate crude ammonium bicarbonate product with a CO2 concentration of about 12%, realizing the direct capture of low-concentration CO2. On the other hand, part of the desulfurized flue gas enters the continuous mineralization reactor, and the fly ash discharged from the coal-fired power plant is controlled to enter the solid leaching reactor and undergoes leaching reaction and filtration treatment with circulating media to obtain Ca-containing products. 2+ Solution containing Ca 2+ The mineralized solution enters a continuous mineralization reactor to mineralize part of the desulfurized flue gas to produce crude calcium carbonate. In other words, this application can simultaneously achieve direct capture of CO2 and mineralization and storage of desulfurized flue gas through fly ash. Compared with the single path in traditional technology, the carbon capture rate of this application is increased by ≥25%, significantly reducing greenhouse gas emissions and achieving both energy-saving and environmental benefits.

[0026] (2) Co-conversion of fly ash and flue gas mineralization: Fly ash containing ≥25wt% CaO discharged from coal-fired power plants is treated by circulating medium leaching reaction and filtration to obtain Ca-containing fly ash. 2+ A solution is used to leach calcium ions, and the solution is mixed with ammonia and a directing agent to enhance crystallization, thus preparing a mineralizing solution. The pH value of the mineralizing solution can be adjusted to contain Ca. 2+ The mineralization solution enters a continuous mineralization reactor, where it comes into contact with and mixes with the counter-currently introduced desulfurized flue gas to carry out a mineralization reaction. This process produces crude calcium carbonate by mineralizing a portion of the desulfurized flue gas, thus simultaneously completing CO2 mineralization and sequestration and fly ash solid waste conversion. Calculations show that this application can achieve CO2 fixation ≥ 0.2t per ton of fly ash, producing crude calcium carbonate (LCC) with a purity > 90%; and purifying the flue gas dust concentration ≤ 5mg / Nm³. 3 SO2 ≤ 35 mg / Nm 3 To achieve ultra-low emissions and resource value-added. Attached Figure Description

[0027] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0028] To gain a more complete understanding of this application and its beneficial effects, the following description will be provided in conjunction with the accompanying drawings. In the following description, the same reference numerals denote the same parts.

[0029] Figure 1 This is a schematic diagram of a coal-fired power plant carbon resource utilization and co-processing system according to an embodiment of this application;

[0030] Figure 2 This is a schematic diagram of the process for the collaborative processing of carbon resources in a coal-fired power plant according to an embodiment of this application.

[0031] Explanation of reference numerals in the attached figures

[0032] 10. Coal-fired power plant carbon resource utilization and co-processing system; 100. Desulfurization tower; 200. Cooling tower; 300. Decarbonization tower; 400. Liquid ammonia reactor; 500. Urea storage tank; 600. Ammonium bicarbonate storage tank; 700. Solid leaching reactor; 800. Continuous mineralization reactor; 900. Ammonium sulfate post-treatment unit; 1000. Two-stage ammonia washing tower; 1100. Mineralization liquid reactor; 1200. Exhaust fan. Detailed Implementation

[0033] To make the above-mentioned objectives, features, and advantages of this application more apparent and understandable, the specific embodiments of this application are described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of this application. However, this application can be implemented in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of this application. Therefore, this application is not limited to the specific embodiments disclosed below.

[0034] In the description of this application, 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", "circumferential", etc., indicating the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this application.

[0035] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "joining," 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 or an electrical connection; 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 expressly limited. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0036] In this application, unless otherwise expressly 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," "on top of," and "over" 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.

[0037] In the description of this application, "several" means one or more, "multiple" means two or more, "greater than," "less than," and "exceeding" are understood to exclude the stated number, while "above," "below," and "within" are understood to include the stated number. The use of "first" and "second" in the description is merely for distinguishing technical features and should not be construed as indicating or implying relative importance, or implicitly indicating the number of indicated technical features, or implicitly indicating the order of the indicated technical features.

[0038] In this document, "optionally," "optionally," and "optional" mean that something is optional, that is, it is selected from either "with" or "without." If multiple "options" appear in a technical solution, unless otherwise specified and there are no contradictions or mutual constraints, each "option" is independent. In this application, descriptions such as "optionally contains" and "optionally includes" indicate "contains or does not contain."

[0039] In this application, unless otherwise stated, the sum of the parts of each component in the composition may be 100 parts by weight. Unless otherwise specified, the percentages (including weight percentages) in this application are based on the total weight of the composition, and "wt%" in this document means mass percentage.

[0040] In this document, unless otherwise stated, the reaction steps may be performed in the order described herein or not. For example, other steps may be included between reaction steps, and the order of reaction steps may be appropriately interchanged. This is something that those skilled in the art can determine based on conventional knowledge and experience. Preferably, the reaction methods described herein are performed sequentially.

[0041] In this application, when numerical intervals (i.e., numerical ranges) are mentioned, unless otherwise specified, the distribution of selectable numerical values ​​within the numerical interval is considered continuous, and includes the two endpoints of the numerical interval (i.e., the minimum and maximum values), as well as every numerical value between these two endpoints. Unless otherwise specified, when a numerical interval refers only to integers within that numerical interval, it includes the two endpoint integers of the numerical range, as well as every integer between the two endpoints, which is equivalent to directly listing every integer. When multiple numerical ranges are provided to describe features or characteristics, these numerical ranges can be merged. In other words, unless otherwise specified, the numerical ranges disclosed in this application should be understood to include any and all subranges included therein. The "numerical value" in the numerical interval can be any quantitative value, such as a number, percentage, ratio, etc. The term "numerical interval" can be broadly included to include percentage intervals, ratio intervals, proportion intervals, etc.

[0042] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0043] This application provides a carbon resource co-processing system 10 for coal-fired power plants, which addresses the environmental pollution and resource waste caused by high energy consumption for CO2 capture and low fly ash utilization in conventional technologies. The carbon resource co-processing system 10 for coal-fired power plants will be described below with reference to the accompanying drawings.

[0044] The coal-fired power plant carbon resource recovery and co-processing system 10 provided in one embodiment of this application is exemplary. Please refer to [link to example]. Figure 1 As shown, Figure 1 This is a schematic diagram of the structure of a coal-fired power plant carbon resource recovery and co-processing system 10 provided in one embodiment of this application. The coal-fired power plant carbon resource recovery and co-processing system 10 of this application can be used for CO2 capture in coal-fired power plants.

[0045] To more clearly illustrate the structure of the coal-fired power plant carbon resource utilization co-processing system 10, the following will introduce the coal-fired power plant carbon resource utilization co-processing system 10 in conjunction with the accompanying drawings.

[0046] For example, please refer to Figure 1 As shown, a coal-fired power plant carbon resource utilization and co-processing system 10 includes a flue gas diversion and desulfurization unit, a carbon dioxide capture and conversion unit, an ammonia recovery unit, and a fly ash mineralization unit.

[0047] The flue gas diversion and desulfurization unit includes a desulfurization tower 100. The desulfurization tower 100 is used to absorb and oxidize the raw flue gas from the coal-fired power plant to form desulfurized flue gas and generate crude ammonium sulfate product.

[0048] The carbon dioxide capture and conversion unit includes a cooling tower 200 and a decarbonization tower 300 connected in sequence. The cooling tower 200 is connected to the desulfurization tower 100 to cool a portion of the desulfurized flue gas from the desulfurization tower 100. The decarbonization tower 300 is used to decarbonize the cooled desulfurized flue gas.

[0049] The ammonia recovery unit is connected to the decarbonization tower 300 so that liquid ammonia is fed into the decarbonization tower 300 to react with carbon dioxide in the decarbonization tower 300 to produce crude ammonium bicarbonate.

[0050] The fly ash mineralization unit includes a solid leaching reactor 700 and a continuous mineralization reactor 800 connected to the solid leaching reactor 700. The solid leaching reactor 700 receives fly ash discharged from a coal-fired power plant and, after leaching and filtration using a circulating medium, obtains a Ca-containing mineralization product. 2+ Solution. A continuous mineralization reactor 800 is connected to a desulfurization tower 100 to utilize solutions containing Ca. 2 + The mineralizing solution reacts with a portion of the desulfurized flue gas from desulfurization tower 100 to produce crude calcium carbonate.

[0051] The aforementioned coal-fired power plant carbon resource recovery and co-processing system 10 is applicable to large-scale resource recovery of carbon dioxide and fly ash. It features low energy consumption and enables simultaneous high-value conversion of CO2 and fly ash, reducing environmental pollution and resource waste. Specifically, the core of this application lies in the cooling and diversion of desulfurized flue gas. Part of the desulfurized flue gas enters the cooling tower 200 for cooling treatment before entering the decarbonization tower 300, while the other part enters the continuous mineralization reactor 800. This achieves simultaneous delivery of desulfurized flue gas to both the decarbonization tower 300 and the continuous mineralization reactor 800, allowing for direct treatment of low-concentration CO2 (e.g., CO2 concentration of 12%~15%) without enrichment. In the first branch, the desulfurized flue gas reacts with liquid ammonia to achieve a carbon capture rate of ≥75%, producing agricultural-grade ammonium bicarbonate with a nitrogen content of ≥17%. In the second branch, the desulfurized flue gas from the legal entity contacts the fly ash-based mineralization liquid in a counter-current manner, simultaneously fixing ≥0.2 t / t of fly ash, producing building-grade light calcium carbonate with a purity >90%.

[0052] In some embodiments, the flue gas diversion and desulfurization unit further includes an induced draft fan 1200; the outlet of the induced draft fan 1200 is connected to the desulfurization tower 100. The induced draft fan 1200 is used to introduce raw flue gas from the coal-fired power plant into the desulfurization tower 100.

[0053] In some embodiments, the desulfurization tower 100 is equipped with a spraying device, which ensures sufficient gas-liquid contact and controls the liquid-to-gas ratio to 8L / m³. 3 ~10L / m 3 Control the SO2 concentration at the outlet of the desulfurization tower 100 to <35 mg / Nm³. 3 At the same time, it cools the flue gas.

[0054] In some embodiments, the decarbonation tower 300 is equipped with a two-stage spraying device. The spraying device enables gas-liquid contact to produce a chemical reaction, fully absorbs carbon dioxide, and produces ammonium bicarbonate product, so that the carbon dioxide removal efficiency in the decarbonation tower 300 is ≥75%.

[0055] In some embodiments, the ammonia recovery unit includes a liquid ammonia reactor 400. The liquid ammonia reactor 400 is connected to a decarbonization tower 300. The liquid ammonia reactor 400 generates liquid ammonia by adding urea and feeds it into the decarbonization tower 300 to react with carbon dioxide within the decarbonization tower 300 to produce crude ammonium bicarbonate.

[0056] In some embodiments, the ammonia recovery unit further includes a urea storage tank 500. The urea storage tank 500 is connected to the liquid ammonia reactor 400 for feeding urea into the liquid ammonia reactor 400;

[0057] In some embodiments, a drive pump is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400.

[0058] In some embodiments, a control valve is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400.

[0059] In some embodiments, a flow detection component is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400. The flow detection component includes a flow meter.

[0060] In some embodiments, the ammonia recovery unit also includes an ammonium bicarbonate storage tank 600. The ammonium bicarbonate storage tank 600 is connected to a decarbonation tower 300 to store crude ammonium bicarbonate.

[0061] In some embodiments, the ammonia recovery unit also includes a centrifuge. The centrifuge is connected between the ammonium bicarbonate storage tank 600 and the decarbonization tower 300, and is used to centrifuge and thicken the crude ammonium bicarbonate.

[0062] In some embodiments, the ammonia recovery unit further includes a two-stage ammonia washing tower 1000. The two-stage ammonia washing tower 1000 is connected to the decarbonization tower 300. The two-stage ammonia washing tower 1000 absorbs the escaped ammonia in the decarbonization tower 300 by adding desulfurization absorbent and then reuses it, and discharges the washed flue gas.

[0063] In some embodiments, the two-stage ammonia washing tower 1000 is also connected to the desulfurization tower 100 to recycle the absorbed liquid ammonia to the desulfurization tower 100 for reuse.

[0064] The aforementioned coal-fired power plant carbon resource utilization and co-processing system 10 achieves the recycling of liquid ammonia through an ammonia circulation mechanism. The two-stage ammonia washing tower 1000 absorbs the escaped ammonia in the decarbonization tower 300 by adding desulfurization absorbent liquid for secondary utilization and discharges the washed flue gas. The recovery rate of the two-stage ammonia washing tower 1000 is >95%, which can be closed-loop with calcium leaching-mineralization reaction. The recycling medium reuse rate is >80%, which significantly reduces operating costs.

[0065] In some embodiments, the coal-fired power plant carbon resource utilization co-processing system 10 further includes an ammonium sulfate post-processing unit 900. The ammonium sulfate post-processing unit 900 is connected to the desulfurization tower 100 and is used to post-process the crude ammonium sulfate product generated from the desulfurization tower 100 after it has been concentrated and crystallized by the heat from the raw flue gas of the coal-fired power plant.

[0066] In some embodiments, the fly ash mineralization unit further includes a mineralization liquid reactor 1100. The mineralization liquid reactor 1100 is connected between the solid leaching reactor 700 and the continuous mineralization reactor 800. The mineralization liquid reactor 1100 processes the fly ash by adding ammonia, a directing agent, and a Ca-containing solution. 2+ The solutions are mixed and the pH is adjusted to form a mineralizing solution for the mineralization reaction.

[0067] In some embodiments, a drive pump is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400.

[0068] In some embodiments, a control valve is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400.

[0069] In some embodiments, a flow detection component is installed on the pipeline between the urea storage tank 500 and the liquid ammonia reactor 400. The flow detection component includes a flow meter.

[0070] The pipelines between desulfurization tower 100 and cooling tower 200, between cooling tower 200 and decarbonization tower 300, between decarbonization tower 300 and liquid ammonia reactor 400, between liquid ammonia reactor 400 and desulfurization tower 100, between desulfurization tower 100 and continuous mineralization reactor 800, and between solid leaching reactor 700 and continuous mineralization reactor 800 are each independently equipped with one or more drive pumps, control valves, and flow meters.

[0071] An embodiment of this application also provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0072] A method for the co-processing of carbon resources in coal-fired power plants, employing the coal-fired power plant carbon resource co-processing system 10 in any of the above embodiments, includes the following steps:

[0073] S10 controls the raw flue gas from the coal-fired power plant to enter the desulfurization tower 100, and controls the desulfurization tower 100 to absorb and oxidize the raw flue gas from the coal-fired power plant to form desulfurized flue gas and generate crude ammonium sulfate products.

[0074] S20. Part of the desulfurized flue gas from the desulfurization tower 100 is cooled in the cooling tower 200 and then enters the decarbonization tower 300. The decarbonization tower 300 is used to decarbonize the cooled flue gas.

[0075] S30, control the ammonia recovery unit to input liquid ammonia into the decarbonization tower 300 to react with carbon dioxide in the decarbonization tower 300 to produce crude ammonium bicarbonate.

[0076] S40. Part of the desulfurized flue gas from the desulfurization tower 100 is controlled to enter the continuous mineralization reactor 800. The fly ash discharged from the coal-fired power plant is controlled to enter the solid leaching reactor 700 and, after leaching reaction and filtration treatment with circulating media, obtain Ca-containing gas. 2+ Solution, control the content of Ca 2+ The mineralized solution enters the continuous mineralization reactor 800 to carry out a mineralization reaction on part of the desulfurized flue gas from the desulfurization tower 100 to produce crude calcium carbonate.

[0077] In some embodiments, the ammonium sulfate post-treatment unit 900 is controlled to post-treat the crude ammonium sulfate product generated from the desulfurization tower 100.

[0078] In some embodiments, escaped ammonia in the decarbonization tower 300 is controlled to enter the two-stage ammonia washing tower 1000. Desulfurization absorbent is added to the two-stage ammonia washing tower 1000 to absorb the escaped ammonia for secondary use, and the washed flue gas is discharged.

[0079] In some embodiments, the liquid ammonia absorbed by the two-stage ammonia washing tower 1000 is controlled to be recycled back into the desulfurization tower 100.

[0080] In some of these implementations, the recycling frequency is not less than once.

[0081] In some implementations, the escaped ammonia concentration is controlled to be ≤3 mg / Nm³. 3 .

[0082] In some embodiments, the crude ammonium bicarbonate generated by the decarbonation tower 300 is centrifuged and thickened before being stored in the ammonium bicarbonate storage tank 600.

[0083] In some embodiments, when controlling the ammonia recovery unit to input liquid ammonia to the decarbonization tower 300, the following steps are included: controlling urea to enter the liquid ammonia reactor 400 and generate liquid ammonia.

[0084] In some embodiments, the circulating medium includes one or more of deionized water, aqueous ethylene glycol solution, and aqueous ethanol solution.

[0085] In some embodiments, the mineralizing solution includes Ca 2+ Solution, ammonia, and directing agent, Ca 2+ The mass ratio of the solution, ammonia, and directing agent is (5~15):(1~3):(0.1~0.2).

[0086] In some embodiments, the directing agent includes one or more of polyacrylamide, sodium dodecylbenzenesulfonate, and trisodium citrate.

[0087] In some embodiments, the pH of the mineralizing solution is controlled to be 9.5 to 10.5.

[0088] In some embodiments, the mineralizing solution is controlled to come into countercurrent contact with the desulfurized flue gas from the desulfurization tower 100.

[0089] In some embodiments, the reaction liquid after the mineralization reaction is subjected to solid-liquid separation treatment to obtain crude calcium carbonate product and flue gas.

[0090] In some embodiments, the mass ratio between fly ash and circulating medium is controlled to be (3~5):1.

[0091] In some of these embodiments, the CaO content in the fly ash is controlled to be above 25%.

[0092] In some embodiments, the leaching reaction temperature is controlled at 40°C to 60°C, and the leaching time is controlled at 2 hours to 4 hours. The leaching reaction temperature can be, but is not limited to, 40°C, 45°C, 50°C, 55°C, 60°C, or any range thereof. The leaching time can be, but is not limited to, 2 hours, 2.5 hours, 3 hours, 3.5 hours, 4 hours, or any range thereof.

[0093] Example 1

[0094] This embodiment provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0095] The method for co-processing carbon resources in coal-fired power plants in this embodiment adopts... Figure 1 The carbon resource recovery and co-processing system 10 shown for coal-fired power plants includes the following steps:

[0096] S110: Control the raw flue gas from the coal-fired power plant to enter the desulfurization tower 100 from the outlet of the induced draft fan 1200. The CO2 concentration in the raw flue gas is between 12% and 15%. The desulfurization tower 100 absorbs and oxidizes the raw flue gas to form desulfurized flue gas and generates crude ammonium sulfate product, removing SO2 from the raw flue gas. X .

[0097] S120, the ammonium sulfate post-processing unit 900 controls the post-processing of the crude ammonium sulfate product generated from the desulfurization tower 100.

[0098] S130: Part of the desulfurized flue gas from the desulfurization tower 100 is cooled in the cooling tower 200 and then enters the decarbonization tower 300. The decarbonization tower 300 is used to decarbonize the cooled flue gas.

[0099] S140. Control the escaped ammonia in the decarbonization tower 300 to enter the two-stage ammonia washing tower 1000. Add desulfurization absorption liquid to the two-stage ammonia washing tower 1000 to absorb the escaped ammonia and reuse it, and discharge the washed flue gas.

[0100] The liquid ammonia absorbed by the two-stage ammonia scrubbing tower 1000 is recycled back to the desulfurization tower 100 for reuse, and the recycling is carried out twice. In this embodiment, the desulfurization flue gas after the decarbonization treatment contains ammonia. At this time, the escaped ammonia can be absorbed a second time by the two-stage ammonia scrubbing tower 1000 to ensure that the ammonia escape rate is controlled at 3 mg / Nm³. 3 The following, after the flue gas has been washed and meets the emission standards, it can be discharged directly.

[0101] S150: Control urea to enter the liquid ammonia reactor 400 and generate liquid ammonia. Control the ammonia recovery unit to input liquid ammonia into the decarbonization tower 300 to react with carbon dioxide in the decarbonization tower 300 to generate crude ammonium bicarbonate. In this embodiment, carbon dioxide in the flue gas reacts with liquid ammonia at room temperature and pressure to generate crude ammonium bicarbonate. After thickening, centrifugation, and other steps, the above-mentioned ammonium bicarbonate product can be generated. Control the crude ammonium bicarbonate generated in the decarbonization tower 300 to undergo centrifugation and thickening treatment before entering the ammonium bicarbonate storage tank 600 for storage.

[0102] S160, containing Ca 2+ A mineralizing solution was prepared by mixing the solution with ammonia and a directing agent, and the pH of the mineralizing solution was adjusted to 10. Ca 2+ The mass ratio of the solution, ammonia, and directing agent is 15:3:0.1. The directing agent includes polyacrylamide.

[0103] Part of the desulfurized flue gas from desulfurization tower 100 is cooled to 15°C before entering continuous mineralization reactor 800, which avoids thermal decomposition and damage to the subsequent reaction end products caused by reaction heat and crystallization heat. Fly ash with a CaO content of over 25% discharged from coal-fired power plants enters solid leaching reactor 700 and undergoes leaching reaction and filtration treatment with circulating media to obtain Ca-containing... 2+ The mass ratio of the solution, fly ash, and circulating medium was 3:1, and the circulating medium included an aqueous ethanol solution. The leaching reaction was carried out at 40°C for 4 hours.

[0104] The mineralized liquid is controlled to enter the continuous mineralization reactor 800. The mineralized liquid is counter-currently contacted with the desulfurized flue gas from the desulfurization tower 100 to carry out a mineralization reaction on a portion of the desulfurized flue gas from the desulfurization tower 100 to produce crude calcium carbonate. The reaction liquid after the mineralization reaction is subjected to solid-liquid separation treatment to obtain the crude calcium carbonate product and flue gas. The purity of CaCO3 in the crude calcium carbonate product is >92%. The recycling rate of the circulating medium is >80%, and the dust concentration in the purified flue gas is <5 mg / Nm³. 3 The flue gas was discharged in compliance with standards after online monitoring.

[0105] Example 2

[0106] This embodiment provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0107] The method for co-processing carbon resources in coal-fired power plants in this embodiment adopts... Figure 1 The carbon resource recovery and co-processing system 10 shown for coal-fired power plants includes the following steps:

[0108] S110: Control the raw flue gas from the coal-fired power plant to enter the desulfurization tower 100 from the outlet of the induced draft fan 1200. The CO2 concentration in the raw flue gas is between 12% and 15%. The desulfurization tower 100 absorbs and oxidizes the raw flue gas to form desulfurized flue gas and generates crude ammonium sulfate product, removing SO2 from the raw flue gas. X .

[0109] S120, the ammonium sulfate post-processing unit 900 controls the post-processing of the crude ammonium sulfate product generated from the desulfurization tower 100.

[0110] S130: Part of the desulfurized flue gas from the desulfurization tower 100 is cooled in the cooling tower 200 and then enters the decarbonization tower 300. The decarbonization tower 300 is used to decarbonize the cooled flue gas.

[0111] S140. Control the escaped ammonia in the decarbonization tower 300 to enter the two-stage ammonia washing tower 1000. Add desulfurization absorption liquid to the two-stage ammonia washing tower 1000 to absorb the escaped ammonia and reuse it, and discharge the washed flue gas.

[0112] The liquid ammonia absorbed by the two-stage ammonia scrubbing tower 1000 is recycled back to the desulfurization tower 100 for reuse, and the recycling is carried out twice. In this embodiment, the desulfurization flue gas after the decarbonization treatment contains ammonia. At this time, the escaped ammonia can be absorbed a second time by the two-stage ammonia scrubbing tower 1000 to ensure that the ammonia escape rate is controlled at 3 mg / Nm³. 3 The following, after the flue gas has been washed and meets the emission standards, it can be discharged directly.

[0113] S150: Control urea to enter the liquid ammonia reactor 400 and generate liquid ammonia. Control the ammonia recovery unit to input liquid ammonia into the decarbonization tower 300 to react with carbon dioxide in the decarbonization tower 300 to generate crude ammonium bicarbonate. In this embodiment, carbon dioxide in the flue gas reacts with liquid ammonia at room temperature and pressure to generate crude ammonium bicarbonate. After thickening, centrifugation, and other steps, the above-mentioned ammonium bicarbonate product can be generated. Control the crude ammonium bicarbonate generated in the decarbonization tower 300 to undergo centrifugation and thickening treatment before entering the ammonium bicarbonate storage tank 600 for storage.

[0114] S160, containing Ca 2+ A mineralizing solution was prepared by mixing the solution with ammonia and a directing agent, and the pH of the mineralizing solution was adjusted to 9.5. 2+ The mass ratio of the solution, ammonia, and directing agent is 15:3:0.2. The directing agent includes polyacrylamide.

[0115] Controlling the temperature of part of the desulfurized flue gas from desulfurization tower 100 to 0℃ before it enters the continuous mineralization reactor 800 can prevent the heat of reaction and crystallization from causing thermal decomposition and damage to the subsequent reaction end products. Controlling the CaO content of fly ash discharged from coal-fired power plants to above 25% before it enters the solid leaching reactor 700 and undergoes leaching reaction and filtration with circulating media to obtain Ca-containing... 2+ The mass ratio of the solution, fly ash, and circulating medium was 3:1, and the circulating medium included an aqueous ethanol solution. The leaching reaction was carried out at 60°C for 2 hours.

[0116] The mineralized liquid is controlled to enter the continuous mineralization reactor 800. The mineralized liquid is counter-currently contacted with the desulfurized flue gas from the desulfurization tower 100 to carry out a mineralization reaction on a portion of the desulfurized flue gas from the desulfurization tower 100 to produce crude calcium carbonate. The reaction liquid after the mineralization reaction undergoes solid-liquid separation treatment to obtain the crude calcium carbonate product and flue gas. The purity of CaCO3 in the crude calcium carbonate product is >93%. The recycling rate of the circulating medium is >81%, and the dust concentration in the purified flue gas is <4.8 mg / Nm³. 3 The flue gas was discharged in compliance with standards after online monitoring.

[0117] Comparative Example 1

[0118] Comparative Example 1 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0119] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The carbon resource utilization and co-processing system of the coal-fired power plant shown has basically the same steps as that in Example 1. The difference is that in this comparative example, the mass ratio between fly ash and circulating medium is 2:1, that is, the fly ash content is too low.

[0120] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 91.8%, and the escaped ammonia concentration was 8 mg / Nm³. 3 Comparative Example 1 shows that when the fly ash content is too low, the purity of CaCO3 does not meet the requirements, the system's adsorption capacity is insufficient, the ammonia retention capacity decreases, and the escaped ammonia concentration is relatively high.

[0121] Comparative Example 2

[0122] Comparative Example 2 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0123] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The carbon resource utilization and co-processing system of the coal-fired power plant shown has basically the same steps as that in Example 1. The difference is that in this comparative example, the mass ratio between fly ash and circulating medium is 6:1, that is, the fly ash content is too high.

[0124] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 87.3%, and the escaped ammonia concentration was 13 mg / Nm³. 3 Comparative Example 1 shows that when the fly ash content is too high, the excessive amount of fly ash will introduce more impurities (such as silicon and aluminum oxides), leading to a decrease in the purity of CaCO3. At the same time, the excessive solid particles will disrupt the homogeneity of the system, resulting in a higher concentration of escaped ammonia.

[0125] Comparative Example 3

[0126] Comparative Example 3 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0127] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The carbon resource utilization and co-processing system of the coal-fired power plant shown has basically the same steps as in Example 1. The difference is that the content of the directing agent in this comparative example is 0.05wt%, which means that the content of the directing agent is too low.

[0128] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 89.5%, and the escaped ammonia concentration was 6 mg / Nm³. 3 Comparative Example 1 shows that when the content of the directing agent is too low, the CaCO3 crystallization process is disordered, easily encapsulates impurities, reduces purity, has little impact on ammonia escape, but the concentration of escaped ammonia is slightly higher.

[0129] Comparative Example 4

[0130] Comparative Example 4 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0131] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The carbon resource utilization and co-processing system of the coal-fired power plant shown has basically the same steps as in Example 1. The difference is that the content of the directing agent in this comparative example is 0.3wt%, which means that the content of the directing agent is too high.

[0132] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 91.4%, and the escaped ammonia concentration was 4 mg / Nm³. 3 Comparative Example 1 shows that when the content of the directing agent is too high, the effect on purity is limited, the purity of CaCO3 does not meet the requirements, but it may increase the viscosity of the system, slightly promote the volatilization of ammonia, and result in a higher concentration of escaped ammonia.

[0133] Comparative Example 5

[0134] Comparative Example 5 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0135] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1The coal-fired power plant carbon resource co-processing system shown has basically the same steps as Example 2, except that the pH value of the mineralizing solution in this comparative example is 8.5.

[0136] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 90.2%, and the escaped ammonia concentration was 10 mg / Nm³. 3 Comparative Example 1 shows that when the pH of the solution is 8.5, that is, when the pH is acidic, it is not conducive to CO2 absorption and calcium carbonate formation, and the incomplete reaction leads to a decrease in purity; ammonia is more volatile in an acidic environment, and the concentration of escaped ammonia increases.

[0137] Comparative Example 6

[0138] Comparative Example 6 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0139] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The coal-fired power plant carbon resource co-processing system shown has basically the same steps as Example 2, except that the pH value of the mineralizing solution in this comparative example is 11.

[0140] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 92.6%, and the escaped ammonia concentration was 4 mg / Nm³. 3 Comparative Example 1 shows that when the pH of the mineralization solution is 11, which is slightly alkaline, it is conducive to CO2 conversion, but the high alkalinity may promote the dissolution of impurities in fly ash, resulting in a slight decrease in purity; the alkaline environment inhibits ammonia volatilization, resulting in a lower escape concentration.

[0141] Comparative Example 7

[0142] Comparative Example 7 provides a method for the collaborative processing of carbon resources in coal-fired power plants.

[0143] The comparative example uses a method for the collaborative treatment of carbon resources in coal-fired power plants. Figure 1 The carbon resource utilization and co-processing system of the coal-fired power plant shown has basically the same steps as that in Example 2. The difference is that in this comparative example, the escaped ammonia in the decarbonization tower does not enter the two-stage ammonia washing tower for absorption and treatment.

[0144] Tests showed that the purity of CaCO3 in the crude calcium carbonate product was 91.4%, and the escaped ammonia concentration was 115 mg / Nm³. 3 Comparative Example 1 shows that when the escaped ammonia in the decarbonation tower does not enter the two-stage ammonia washing tower for absorption and treatment, there is no ammonia recovery step, and the escape concentration increases significantly; however, it has little impact on the purity of calcium carbonate.

[0145] In summary, compared with traditional technologies, this application has at least the following beneficial effects:

[0146] (1) Dual-path synergistic carbon capture mechanism: This application sets up a decarbonization tower 300 and a continuous mineralization reactor 800. The flue gas from the coal-fired power plant is absorbed and oxidized in the desulfurization tower 100 to form desulfurized flue gas and generate crude ammonium sulfate product. Part of the desulfurized flue gas enters the cooling tower 200 for cooling treatment and then enters the decarbonization tower 300. Part of the desulfurized flue gas enters the continuous mineralization reactor 800, realizing the simultaneous delivery of desulfurized flue gas to the decarbonization tower 300 and the continuous mineralization reactor 800. On the one hand, the decarbonization tower 300 decarbonizes the cooled desulfurized flue gas and inputs liquid ammonia into the decarbonization tower 300 to react with carbon dioxide in the decarbonization tower 300 to generate crude ammonium bicarbonate product with a CO2 concentration of about 12%, realizing the direct capture of low-concentration CO2. On the other hand, part of the desulfurized flue gas enters the continuous mineralization reactor 800, and controls the fly ash discharged from the coal-fired power plant to enter the solid leaching reactor 700 and obtain Ca-containing products after leaching reaction and filtration treatment by circulating media. 2+ Solution containing Ca 2+ The mineralized solution enters the continuous mineralization reactor 800 to carry out a mineralization reaction on part of the desulfurized flue gas to produce crude calcium carbonate. That is, this application can simultaneously achieve direct capture of CO2 and mineralization and storage of desulfurized flue gas through fly ash. Compared with the single path in traditional technology, the carbon capture rate of this application is increased by ≥25%, significantly reducing greenhouse gas emissions and achieving both energy-saving and environmental protection benefits.

[0147] (2) Co-conversion of fly ash and flue gas mineralization: Fly ash containing ≥25wt% CaO discharged from coal-fired power plants is treated by circulating medium leaching reaction and filtration to obtain Ca-containing fly ash. 2+ A solution is used to leach calcium ions, and the solution is mixed with ammonia and a directing agent to enhance crystallization, thus preparing a mineralizing solution. The pH value of the mineralizing solution can be adjusted to contain Ca. 2+ The mineralization solution enters a continuous mineralization reactor 800, where it comes into contact with and mixes with the counter-currently introduced desulfurized flue gas to carry out a mineralization reaction. This process produces crude calcium carbonate by partially mineralizing the desulfurized flue gas, thus simultaneously completing CO2 mineralization and sequestration and fly ash solid waste conversion. Calculations show that this application can achieve CO2 fixation ≥ 0.2t per ton of fly ash, producing crude calcium carbonate (LCC) with a purity > 90%; and purifying the flue gas dust concentration ≤ 5mg / Nm³. 3 SO2 ≤ 35 mg / Nm 3 To achieve ultra-low emissions and resource value-added.

[0148] In the above embodiments, the descriptions of each embodiment have different focuses. For parts not described in detail in a certain embodiment, please refer to the relevant descriptions in other embodiments.

[0149] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0150] The embodiments described above are merely illustrative of several implementation methods of this application, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of this patent application. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this application, and these all fall within the protection scope of this application. Therefore, the protection scope of this patent application should be determined by the appended claims.

Claims

1. A collaborative carbon resource utilization system for coal-fired power plants, characterized in that, It includes a flue gas diversion and desulfurization unit, a carbon dioxide capture and conversion unit, an ammonia recovery unit, and a fly ash mineralization unit; The flue gas diversion and desulfurization unit includes a desulfurization tower, which is used to absorb and oxidize the raw flue gas from the coal-fired power plant to form desulfurized flue gas and generate crude ammonium sulfate product. The carbon dioxide capture and conversion unit includes a cooling tower and a decarbonization tower connected in sequence. The cooling tower is connected to the desulfurization tower to cool a portion of the desulfurized flue gas from the desulfurization tower, and the decarbonization tower is used to decarbonize the cooled desulfurized flue gas. The ammonia recovery unit is connected to the decarbonization tower so that liquid ammonia is fed into the decarbonization tower to react with carbon dioxide in the decarbonization tower to produce crude ammonium bicarbonate. The fly ash mineralization unit includes a solid leaching reactor and a continuous mineralization reactor connected to the solid leaching reactor. The solid leaching reactor is used to receive fly ash discharged from a coal-fired power plant and, after leaching and filtration with a circulating medium, obtain Ca-containing fly ash. 2+ The solution, the continuous mineralization reactor connected to the desulfurization tower, utilizes the solution containing Ca. 2+ The mineralizing solution reacts with a portion of the desulfurized flue gas from the desulfurization tower to produce crude calcium carbonate.

2. The coal-fired power plant carbon resource utilization and co-processing system according to claim 1, characterized in that, The ammonia recovery unit includes a liquid ammonia reactor connected to the decarbonization tower. The liquid ammonia reactor generates liquid ammonia by adding urea and inputs it into the decarbonization tower to react with carbon dioxide in the decarbonization tower to generate crude ammonium bicarbonate.

3. The coal-fired power plant carbon resource utilization and co-processing system according to claim 2, characterized in that, The coal-fired power plant carbon resource utilization and co-processing system meets at least one of the following conditions: (1) The ammonia recovery unit further includes a urea storage tank, which is connected to the liquid ammonia reactor for inputting urea into the liquid ammonia reactor; (2) The ammonia recovery unit further includes an ammonium bicarbonate storage tank, which is connected to the decarbonation tower to store the crude ammonium bicarbonate.

4. The coal-fired power plant carbon resource utilization and co-processing system according to claim 3, characterized in that, The coal-fired power plant carbon resource utilization and co-processing system meets at least one of the following conditions: (1) A drive pump is installed on the pipeline between the urea storage tank and the liquid ammonia reactor; (2) A control valve is installed on the pipeline between the urea storage tank and the liquid ammonia reactor.

5. The coal-fired power plant carbon resource utilization and co-processing system according to claim 3, characterized in that, A flow detection device is installed on the pipeline between the urea storage tank and the liquid ammonia reactor.

6. The coal-fired power plant carbon resource utilization and co-processing system according to claim 3, characterized in that, The ammonia recovery unit also includes a centrifuge device connected between the ammonium bicarbonate storage tank and the decarbonization tower. The centrifuge device is used to centrifuge and thicken the crude ammonium bicarbonate.

7. The coal-fired power plant carbon resource utilization and co-processing system according to claim 1, characterized in that, The ammonia recovery unit also includes a two-stage ammonia washing tower connected to the decarbonization tower. The two-stage ammonia washing tower absorbs the escaped ammonia in the decarbonization tower by adding desulfurization absorbent for secondary use, and discharges the washed flue gas.

8. The coal-fired power plant carbon resource utilization and co-processing system according to claim 7, characterized in that, The two-stage ammonia washing tower is also connected to the desulfurization tower to recycle the absorbed liquid ammonia back to the desulfurization tower for reuse.

9. The coal-fired power plant carbon resource utilization and co-processing system according to any one of claims 1 to 8, characterized in that, The coal-fired power plant carbon resource utilization co-processing system also includes an ammonium sulfate post-processing unit, which is connected to the desulfurization tower. The ammonium sulfate post-processing unit is used to post-process the crude ammonium sulfate product generated from the desulfurization tower after it has been concentrated and crystallized by the heat of the raw flue gas from the coal-fired power plant.

10. The coal-fired power plant carbon resource utilization and co-processing system according to any one of claims 1 to 8, characterized in that, The fly ash mineralization unit further includes a mineralization liquid reactor, which is connected between the solid leaching reactor and the continuous mineralization reactor. The mineralization liquid reactor is activated by adding ammonia water, a directing agent, and Ca-containing... 2+ The solutions are mixed and the pH is adjusted to form the mineralizing solution used for the mineralization reaction.

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