Coal-fired power plant low-carbonization emission system and coal-fired power plant low-carbonization emission treatment method

Abstract

The invention relates to the technical field of carbon treatment, in particular to a coal-fired power plant low-carbonization emission system and a coal-fired power plant low-carbonization emission treatment method. A coal-fired power plant low-carbonization emission system comprises a combustion device connected with a pretreatment device; the flue gas purification device comprises a dust removal mechanism, a desulfurization mechanism and a denitration mechanism which are sequentially connected, the dust removal mechanism is connected with the combustion device, flue gas component monitoring mechanisms are arranged between the dust removal mechanism and the desulfurization mechanism and between the desulfurization mechanism and the denitration mechanism, and the flue gas component monitoring mechanisms are suitable for monitoring operation parameters of the dust removal mechanism and the desulfurization mechanism. The controller adjusts the operation parameters of the desulfurization mechanism and the denitration mechanism according to the monitoring result; the carbon dioxide trapping device is connected with the denitration mechanism; and the carbon dioxide utilization and storage device is connected with the carbon dioxide trapping device. The problems that carbon dioxide cannot be converted during flue gas emission of an existing coal-fired power plant, and the energy utilization rate is low are solved.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon treatment, and in particular to a low-carbon emission system and a low-carbon emission treatment method for a coal-fired power plant. Background Art

[0002] A thermal power plant, also known as a thermal power plant, uses combustible materials (such as coal) as fuel to produce electricity. The basic production process is as follows: The fuel burns, heating water to generate steam, converting the fuel's chemical energy into thermal energy. The steam pressure then drives a turbine, converting the thermal energy into mechanical energy. The turbine then drives a generator, converting the mechanical energy into electrical energy.

[0003] Currently, existing coal-fired power plants undergo a series of treatment processes before direct flue gas discharge. These treatments aim to remove harmful substances such as sulfur oxides and particulate matter to meet environmental standards. However, a major issue arises when it comes to the treatment of CO2 in flue gas. While basic CO2 treatment is performed, the focus is primarily on CO2 removal rather than conversion. This results in a significant amount of CO2 being wasted in the flue gas, hindering its subsequent reuse. Summary of the Invention

[0004] In view of this, the present invention provides a low-carbon emission system and a low-carbon emission treatment method for a coal-fired power plant to solve the problem that the existing coal-fired power plant cannot convert and treat carbon dioxide during flue gas emissions and has low energy utilization.

[0005] In a first aspect, the present invention provides a low-carbon emission system for a coal-fired power plant, comprising:

[0006] Pre-processing device, suitable for pre-processing raw coal and then transporting it to the next process;

[0007] The combustion device is connected to the pre-treatment device and is suitable for mixing the raw coal and the combustion-supporting gas and then performing combustion treatment;

[0008] The flue gas purification device includes a dust removal mechanism, a desulfurization mechanism, and a denitrification mechanism that are sequentially connected. The dust removal mechanism is connected to the combustion device. A flue gas composition monitoring mechanism is provided between the dust removal mechanism and the desulfurization mechanism, and between the desulfurization mechanism and the denitrification mechanism. The flue gas composition monitoring mechanism is adapted to monitor operating parameters of the dust removal mechanism and the desulfurization mechanism and transmit the information to a controller. The controller adjusts the operating parameters of the desulfurization mechanism and the denitrification mechanism according to the monitoring results.

[0009] A carbon dioxide capture device, connected to the denitrification mechanism, suitable for capturing carbon dioxide in the flue gas output by the denitrification mechanism;

[0010] The carbon dioxide utilization and storage device is connected to the carbon dioxide capture device and is suitable for reusing or storing the carbon dioxide captured by the carbon dioxide capture device.

[0011] The low-carbon emission system for coal-fired power plants provided by the present invention is characterized in that the pre-treated raw coal is mixed with a combustion-supporting gas in a combustion device and then burned, and the flue gas generated by the combustion is sequentially subjected to dust removal, desulfurization and denitrification treatments by a dust removal mechanism, a desulfurization mechanism and a denitrification mechanism. While the above treatments are being performed, a flue gas composition monitoring mechanism monitors the operating parameters of the dust removal mechanism and the desulfurization mechanism in real time, and sends the results to a controller. The controller adjusts the operating parameters of the desulfurization mechanism and the denitrification mechanism according to the monitoring results, thereby achieving coordinated and efficient operation among the various mechanisms of the flue gas purification device, ensuring that the overall purification efficiency is always maintained at a high level, effectively reducing the emission of harmful gases and dust, and helping coal-fired power plants achieve low-carbon emission goals. The flue gas that has undergone the above treatment is captured by a carbon dioxide capture device and then transported to a carbon dioxide utilization and storage device, which can be used for chemical production of urea, carbonation of food and beverages, and agricultural greenhouse fertilization. Temporarily unused carbon dioxide can be injected into underground saline layers or abandoned oil and gas fields through injection wells, thereby converting the carbon dioxide in the flue gas and improving energy utilization.

[0012] In an optional embodiment, the carbon dioxide utilization and storage device includes a seismic monitor, a water quality sensor, a flow monitor, a carbon dioxide delivery pipeline, and a pressure and flow stabilization structure provided on the carbon dioxide delivery pipeline.

[0013] Seismic monitors monitor tiny earthquake activities in underground storage areas in real time; groundwater testing using a combination of water quality sensors and flow monitors can promptly detect abnormal groundwater quality or flow caused by carbon dioxide leakage, ensuring storage safety; the pressure and flow stabilization structure monitors the pressure and flow on the carbon dioxide transmission pipeline in real time to ensure the continuity of chemical production.

[0014] In an optional embodiment, the carbon dioxide capture device includes a chemical absorption structure, a physical adsorption structure and a membrane separation structure, and switching valves are provided between the chemical absorption structure, the physical adsorption structure and the membrane separation structure, and the switching valves are all connected to the controller signal.

[0015] Chemical absorption structure, physical adsorption structure and membrane separation structure can be flexibly combined and operated by switching valves according to the carbon dioxide concentration, flow rate and cost-benefit analysis results in the flue gas. They can make full use of the characteristics of different capture structures, optimize carbon dioxide capture according to actual operating conditions, improve capture efficiency, reduce capture costs, and effectively promote carbon dioxide emission reduction and low-carbon development of coal-fired power plants.

[0016] In an optional embodiment, the chemical absorption structure includes an absorption tower and a regeneration tower, the physical adsorption structure is activated carbon, and the membrane separation structure is a polyimide membrane.

[0017] In the absorption tower, specific temperature and pressure conditions can promote the forward reaction, while in the regeneration tower, by changing the temperature and other conditions, the reaction can be reversed to release high-purity carbon dioxide; activated carbon can effectively adsorb carbon dioxide due to its huge specific surface area and rich pore structure; organic membranes such as polyimide have good chemical stability and gas separation performance, but in actual applications, factors such as the membrane's pressure resistance, flux, and long-term stability need to be considered.

[0018] In an optional embodiment, the dust removal mechanism includes an electrostatic precipitator and a bag dust collector, the desulfurization mechanism includes a desulfurization tower and a spray pump, and the denitrification mechanism includes a denitrification reactor and a gas branch pipe provided on the denitrification reactor.

[0019] The electrostatic precipitator uses discharge and collection electrodes to charge dust and then deposit it, achieving a dust removal efficiency of over 99% for dust particles between 0.01μm and 10μm. The bag filter uses pulse jet cleaning to achieve a filtration efficiency of over 99.9% for dust particles larger than 0.5μm. The desulfurization structure adopts limestone-gypsum wet desulfurization or ammonia desulfurization. The limestone-gypsum wet desulfurization reacts limestone slurry with flue gas in an absorption tower, achieving a desulfurization efficiency of 95%-99%. The ammonia desulfurization uses ammonia solution to absorb sulfur dioxide to produce ammonium sulfate as a fertilizer raw material, achieving resource recycling and desulfurization efficiency of 90%-98%. The denitrification mechanism uses selective catalytic reduction to denitrify. At temperatures of 280°C to 420°C, ammonia reacts with nitrogen oxides using vanadium-titanium catalysts, achieving a denitrification efficiency of 80%-95%. Nitrogen oxides are reduced to nitrogen and water, effectively reducing nitrogen oxide emissions.

[0020] In an optional embodiment, the combustion device includes a low-nitrogen burner and a staged combustion structure that are interconnected, and a plurality of fuel nozzles and air nozzles are staggeredly arranged on the combustion head of the low-nitrogen burner.

[0021] The unique staggered arrangement of fuel and air nozzles in the low-nitrogen burner allows the fuel to burn in an oxygen-deficient environment in the fuel-rich zone, fundamentally suppressing the generation of thermal nitrogen oxides. Air is then added to the fuel-lean zone to ensure complete combustion of the fuel, improving combustion efficiency while significantly reducing the generation of nitrogen oxides. The graded combustion structure rationally distributes the air volume to different areas of the furnace, forming a fuel-rich combustion zone in the main combustion zone, allowing the fuel to be fully preheated and initially burned, reducing the generation of nitrogen oxides. The remaining air is added to the burnout zone to ensure that incompletely burned substances are fully burned, further reducing nitrogen oxide emissions. The synergistic effect of these two technologies has significantly reduced the emission of nitrogen oxides, a major pollutant, which is conducive to improving the quality of the atmospheric environment and helping coal-fired power plants develop in a low-carbon and clean direction.

[0022] In an optional embodiment, the low-nitrogen burner and the staged combustion mechanism are both connected to a combustion parameter monitoring structure, and the combustion parameter monitoring structure is connected to the burner and the supporting gas supply device.

[0023] Both the low-nitrogen burner and the staged combustion structure are connected to a combustion parameter monitoring structure to monitor parameters such as combustion temperature, fuel and gas ratio in real time, and provide feedback to adjust the operation of the burner and gas supply device. This is because combustion temperature has a key impact on combustion efficiency and nitrogen oxide generation. When the combustion temperature is too high, it may cause a significant increase in nitrogen oxide generation. At this time, the monitoring structure will feedback signals to the burner and gas supply device to reduce the power of the burner or increase the gas supply to reduce the combustion temperature.

[0024] In a second aspect, the present invention further provides a method for treating low-carbon emissions from coal-fired power plants, which utilizes a low-carbon emission system of a coal-fired power plant for treatment, comprising the following steps:

[0025] The pre-treated raw coal is mixed with the combustion-supporting gas and ignited to produce flue gas;

[0026] The flue gas is subjected to dust removal, desulfurization and denitrification treatment in sequence, while the composition of the flue gas after each treatment step is monitored, and the treatment parameters of the next step are adjusted according to the monitoring results;

[0027] Capture carbon dioxide from flue gas;

[0028] The captured carbon dioxide is reused or stored.

[0029] In an optional embodiment, when the amount of dust in the flue gas after dust removal exceeds the first predetermined value of the desulfurization treatment, the spray flow rate is increased by 10%-20% or the concentration of the absorbent is increased by 5%-10%; when the sulfur dioxide content after desulfurization exceeds the second predetermined value of the denitrification treatment, the injection amount of ammonia is increased by 5%-10% or the temperature is increased by 20°C.

[0030] By increasing the spray flow rate, the amount of slurry sprayed into the absorption tower per unit time is increased, the dust washing effect is enhanced, and the concentration of the absorbent is increased to replenish the absorbent consumed by the influence of dust, ensuring the full progress of the desulfurization reaction; the ammonia injection volume is increased to ensure that there is enough ammonia to react with nitrogen oxides. Raising the temperature can optimize the activity of the catalyst, increase the catalyst's tolerance to sulfur dioxide, and promote the denitrification reaction.

[0031] In an optional embodiment, the combustion temperature of the raw coal and the supporting gas is 1300° C.-1400° C., the power adjustment range of the burner is 30%-100%, and the supply amount adjustment range of the supporting gas is 70%-150%.

[0032] Within this combustion temperature range, the coal can be fully burned to maintain the power generation efficiency of the power plant, and the generation of thermal nitrogen oxides can be effectively reduced; the supply adjustment range of the supporting combustion gas ensures the stability and sufficiency of the combustion. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0034] Figure 1 This is a schematic diagram of the principle of a combustion device according to an embodiment of the present invention;

[0035] Figure 2 This is a schematic diagram of the principle of a flue gas purification device according to an embodiment of the present invention;

[0036] Figure 3 This is a schematic diagram of the principle of a carbon dioxide capture device according to an embodiment of the present invention;

[0037] Figure 4 Schematic diagram of the principle of a carbon dioxide utilization and storage device according to an embodiment of the present invention. DETAILED DESCRIPTION

[0038] To make the purpose, technical solutions, and advantages of the embodiments of the present invention more clear, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without making creative efforts shall fall within the scope of protection of the present invention.

[0039] The following combination Figures 1 to 4, describing embodiments of the present invention.

[0040] According to an embodiment of the present invention, a low-carbon emission system for a coal-fired power plant is provided, comprising:

[0041] Pre-processing device, suitable for pre-processing raw coal and then transporting it to the next process;

[0042] The combustion device is connected to the pre-treatment device and is suitable for mixing the raw coal and the combustion-supporting gas and then performing combustion treatment;

[0043] The flue gas purification device includes a dust removal mechanism, a desulfurization mechanism, and a denitrification mechanism that are sequentially connected. The dust removal mechanism is connected to the combustion device. A flue gas composition monitoring mechanism is provided between the dust removal mechanism and the desulfurization mechanism, and between the desulfurization mechanism and the denitrification mechanism. The flue gas composition monitoring mechanism is adapted to monitor operating parameters of the dust removal mechanism and the desulfurization mechanism and transmit the information to a controller. The controller adjusts the operating parameters of the desulfurization mechanism and the denitrification mechanism according to the monitoring results.

[0044] A carbon dioxide capture device, connected to the denitrification mechanism, suitable for capturing carbon dioxide in the flue gas output by the denitrification mechanism;

[0045] The carbon dioxide utilization and storage device is connected to the carbon dioxide capture device and is suitable for reusing or storing the carbon dioxide captured by the carbon dioxide capture device.

[0046] The pre-processing unit includes a crushing mechanism, a screening mechanism, and a washing mechanism. The raw coal first enters the crushing mechanism, where it is coarsely crushed by jaw crushers and cone crushers, and then finely crushed by impact crushers and hammer crushers. The goal is to crush the coal into an appropriate particle size for subsequent processes. The crushed coal then enters the screening mechanism, where it is graded by particle size using a vibrating screen or circular vibrating screen. Coal that does not meet the particle size requirements is returned to the crushing mechanism for reprocessing to ensure consistent particle size. The screened coal then enters the washing mechanism, where a combination of jig washing and heavy media washing is used to remove impurities, reducing the coal's ash content by 10%-30% and its sulfur content by 30%-70%. Flow monitoring and regulation devices are installed on the pipelines connecting the crushing, screening, and washing units to monitor coal flow and particle size in real time. Based on the monitoring results, they automatically adjust the operating parameters of each unit. For example, when the coal flow rate changes, the device automatically adjusts operating parameters such as the crusher speed, the vibrating screen amplitude, and the washing unit's processing capacity, ensuring stable and efficient operation of each unit. When the coal flow rate increases, the crusher speed is increased to accelerate crushing; the vibrating screen amplitude is increased to improve screening efficiency; and the washing unit's processing capacity is increased, ensuring a smooth pretreatment process. If the coal particle size does not meet expectations, the flow monitoring and regulation device uses this feedback to adjust the crusher type or washing process parameters to ensure that the final pretreated coal quality meets the requirements. This automated regulation mechanism improves the operational stability and production efficiency of the coal pretreatment module, reduces manual intervention, and ensures consistent coal pretreatment results, laying a good foundation for subsequent efficient combustion and low carbon emissions.

[0047] The pretreated coal enters the combustion device and first burns in the fuel-rich zone under oxygen to suppress the generation of thermal nitrogen oxides. Then, a combustion-supporting gas is added in the fuel-lean zone to achieve complete combustion, reducing the generation of nitrogen oxides by 30%-60%. In this embodiment, the combustion-supporting gas is air, and oxygen can also be selected as needed.

[0048] The flue gas generated by combustion first enters the dust removal unit for dust removal. The desulfurization unit, which uses either limestone-gypsum wet desulfurization or ammonia-based desulfurization, then enters the denitrification unit, where selective catalytic reduction (SCR) is used for denitrification. Between the dust removal and desulfurization units, and between the desulfurization and denitrification units, a flue gas composition monitoring unit monitors the operating parameters of the dust removal and desulfurization units in real time and transmits these data to a controller. The controller adjusts these parameters based on the monitoring results to ensure overall flue gas purification efficiency. The flue gas composition monitoring unit plays a key role as a bridge and coordinator within the flue gas purification system. After the dust removal unit begins operating, it immediately tests the purified flue gas composition to determine whether excessive dust or other impurities are present. If high dust levels are detected, this information is fed back to the desulfurization unit, which can then adjust parameters such as spray intensity and absorbent dosage to address the potential impact of excessive dust on desulfurization performance. When the desulfurization mechanism completes its work, the flue gas composition monitoring mechanism will again detect the content of sulfur dioxide and other components in the flue gas. If the sulfur dioxide content exceeds expectations, the denitrification mechanism will be notified to adjust the catalyst activity, ammonia injection volume and other operating parameters to ensure that possible residual sulfur dioxide and other pollutants can be treated simultaneously during the denitrification process.

[0049] After denitrification, the flue gas enters the CO2 capture device. Based on the CO2 concentration and flow rate in the flue gas, as well as the results of a cost-benefit analysis, an appropriate capture method or combination is selected. The captured CO2 is then transported to the CO2 utilization and storage device.

[0050] The low-carbon emission system for coal-fired power plants provided by the present invention is characterized in that the raw coal that has been pre-treated is mixed with the combustion-supporting gas in the combustion device and then burned. The flue gas generated by the combustion is sequentially subjected to dust removal, desulfurization and denitrification treatment by a dust removal mechanism, a desulfurization mechanism and a denitrification mechanism. While the above treatment is being carried out, the flue gas composition monitoring mechanism monitors the operating parameters of the dust removal mechanism and the desulfurization mechanism in real time and sends them to the controller. The controller adjusts the operating parameters of the desulfurization mechanism and the denitrification mechanism according to the monitoring results, thereby achieving coordinated and efficient operation between the various mechanisms of the flue gas purification device, ensuring that the overall purification efficiency is always maintained at a high level, effectively reducing the emission of harmful gases and dust, and helping coal-fired power plants achieve low-carbon emission goals. The flue gas that has undergone the above treatment is captured by the carbon dioxide capture device and then transported to the carbon dioxide utilization and storage device, which can be used for chemical production of urea, carbonation of food and beverages, and agricultural greenhouse fertilization, etc. The temporarily unused carbon dioxide can be injected into underground saline aquifers or abandoned oil and gas fields through injection wells, thereby converting the carbon dioxide in the flue gas and improving energy utilization.

[0051] In one embodiment, a carbon dioxide utilization and storage device includes a seismic monitor, a water quality sensor, a flow monitor, a carbon dioxide delivery pipeline, and a pressure and flow stabilization structure provided on the carbon dioxide delivery pipeline.

[0052] Chemical production processes require extremely high raw material stability. A stable supply of carbon dioxide ensures continuous production and consistent product quality. Carbon dioxide can be directly applied to urea production during carbon dioxide recovery. The stable carbon dioxide flow and pressure ensure that the reaction proceeds according to the set process parameters, avoiding incomplete reactions or product quality degradation caused by fluctuations in the carbon dioxide supply. In the field of carbon dioxide storage, microseismic monitoring technology can monitor small earthquakes in underground storage areas in real time, promptly detecting potential changes in the formations caused by carbon dioxide injection, such as fault activity, and providing early warning for storage safety. Groundwater monitoring methods that combine water quality sensors and flow monitors can accurately monitor the concentrations of various chemical substances in groundwater and changes in water flow. If abnormal groundwater quality or flow due to carbon dioxide leakage is detected, timely measures can be taken to ensure the safety of the groundwater environment in the storage area. These technical measures jointly ensure the safe and stable operation of carbon dioxide utilization and storage equipment, providing important support for the integrity and sustainability of low-carbon emission systems in coal-fired power plants.

[0053] Seismic monitors monitor tiny earthquake activities in underground storage areas in real time; groundwater testing using a combination of water quality sensors and flow monitors can promptly detect abnormal groundwater quality or flow caused by carbon dioxide leakage, ensuring storage safety; the pressure and flow stabilization structure monitors the pressure and flow on the carbon dioxide transmission pipeline in real time to ensure the continuity of chemical production.

[0054] In one embodiment, the carbon dioxide capture device includes a chemical absorption structure, a physical adsorption structure and a membrane separation structure. Switching valves are provided between the chemical absorption structure, the physical adsorption structure and the membrane separation structure, and the switching valves are all connected to the controller signal.

[0055] When the flue gas CO2 concentration is high and the flow rate is stable, chemical absorption structures are preferred for treatment due to their high capture efficiency and ability to recover large quantities of CO2. If the CO2 concentration is low and the flow rate fluctuates significantly, physical adsorption structures are more suitable, as they can flexibly adapt to changing operating conditions. Membrane separation structures offer unique advantages in certain scenarios, such as those with strict floor space requirements and energy consumption concerns. In actual operation, multiple capture structures can be combined based on cost-benefit analysis results, initially using membrane separation structures for initial separation to reduce CO2 concentration, followed by deep capture using chemical absorption structures or physical adsorption structures to achieve optimal capture efficiency. When the flue gas CO2 concentration is high and the flow rate is high, if the cost-benefit analysis shows that the chemical absorption structure is more economical and efficient, the controller can switch the valve to direct the flue gas into the chemical absorption structure for capture, fully leveraging its high capture efficiency. If the CO2 concentration is low and the flow rate is unstable, the cost-benefit analysis suggests that the physical adsorption structure may be more suitable, and the controller will switch the valve to allow the flue gas to enter the physical adsorption structure for capture. In some cases, membrane separation structures may offer cost advantages within specific CO2 concentration and flow rates, allowing the controller to make timely adjustments, directing flue gas to the membrane separation structure for capture. It's even possible to combine multiple capture methods based on actual conditions, such as using a membrane separation structure for initial separation and then using a chemical absorption structure for deep capture of the remaining high-concentration CO2. This flexible combination of operations fully leverages the characteristics of different capture methods, optimizing CO2 capture based on actual operating conditions, improving capture efficiency, and reducing capture costs, effectively promoting CO2 emission reduction and low-carbon development in coal-fired power plants. During peak daytime electricity consumption, when power generation is high and CO2 concentrations in flue gas are high and flow rates are high, the controller directs most of the flue gas to the chemical absorption structure for capture. During low nighttime electricity consumption, when power generation decreases, flue gas volume and CO2 concentrations decrease, and flow rates are unstable, the controller switches valves to direct flue gas primarily to the physical absorption structure for capture. In some special cases, such as when a power plant undergoes equipment maintenance resulting in large fluctuations in flue gas composition and flow, a cost-benefit analysis is conducted and a membrane separation structure combined with a chemical absorption structure is adopted. The membrane separation structure is first used for rapid preliminary separation, and then the chemical absorption structure is used for deep treatment, which not only ensures capture efficiency but also reduces operating costs.

[0056] Chemical absorption structure, physical adsorption structure and membrane separation structure can be flexibly combined and operated by switching valves according to the carbon dioxide concentration, flow rate and cost-benefit analysis results in the flue gas. They can make full use of the characteristics of different capture structures, optimize carbon dioxide capture according to actual operating conditions, improve capture efficiency, reduce capture costs, and effectively promote carbon dioxide emission reduction and low-carbon development of coal-fired power plants.

[0057] In one embodiment, the chemical absorption structure includes an absorption tower and a regeneration tower, the physical adsorption structure is activated carbon, and the membrane separation structure is a polyimide membrane.

[0058] In the chemical absorption structure, ethanolamine solution is used to absorb carbon dioxide in the absorption tower to generate carbamate, which is then heated to 100°C-120°C in the regeneration tower to desorb carbon dioxide, with a capture efficiency of up to 90%-95%. In the physical adsorption structure, activated carbon adsorption is used to desorb carbon dioxide by increasing the temperature or reducing the pressure, with a capture efficiency of up to 80%-90%. In the membrane separation structure, organic membranes such as polyimide membranes are used to achieve selective permeation of carbon dioxide under pressure difference, with a capture efficiency of 70%-85%.

[0059] Among them, in the chemical absorption structure, the reaction between ethanolamine solution and carbon dioxide is a reversible process.

[0060] Within the absorption tower, specific temperature and pressure conditions promote the forward reaction. Specifically, the temperature range for the chemical reaction between carbon dioxide and ethanolamine solution to proceed in the forward direction is typically 40°C-60°C. Within this temperature range, the ethanolamine solution achieves an ideal absorption rate and amount of carbon dioxide. Excessively low temperatures significantly slow the reaction rate and reduce absorption efficiency; excessively high temperatures increase ethanolamine volatilization losses and hinder carbon dioxide absorption. Pressure is generally maintained between ambient and slightly positive, ranging from approximately 1 to 3 standard atmospheres (101.325-303.975 kPa). In the regeneration tower, the carbamate formed after carbon dioxide absorption is decomposed and desorbed by varying the temperature. The temperature must be heated to 100°C-120°C, which provides sufficient energy for the reverse reaction to occur, effectively desorbing carbon dioxide from the solution. When the temperature is below 100°C, the desorption reaction is slow to proceed, resulting in a low amount of CO2 desorbed. Temperatures above 120°C, while the desorption rate is accelerated, can exacerbate ethanolamine degradation, shorten the absorbent's service life, and increase energy consumption. In physical adsorption structures, the adsorption performance of activated carbon is closely related to its pore structure. Activated carbons with different pore size distributions exhibit varying amounts and rates of CO2 adsorption. The key to membrane separation lies in the selection of membrane materials and the design of the membrane assembly. Chemical absorption structures utilize the high affinity of ethanolamine solutions for CO2 to effectively absorb CO2 within the absorption tower and convert it into carbamate. Heating to a specific temperature range in the regeneration tower decomposes the carbamate, desorbing high-purity CO2. High capture efficiency ensures high CO2 recovery. In physical adsorption structures, CO2 desorption is achieved by increasing the temperature or decreasing the pressure to alter the adsorption equilibrium, resulting in high capture efficiency. Membrane separation structures exploit the differential permselectivity of organic membranes, such as polyimide, for different gas molecules. Driven by a pressure differential, CO2 preferentially passes through the membrane, achieving separation and capture. These three capture methods each have their own advantages, providing diverse options for carbon dioxide capture under different operating conditions and needs, helping to improve the overall efficiency and economy of carbon dioxide capture and promote the low-carbon transformation of coal-fired power plants.

[0061] In the absorption tower, specific temperature and pressure conditions can promote the forward reaction, while in the regeneration tower, by changing the temperature and other conditions, the reaction can be reversed to release high-purity carbon dioxide; activated carbon can effectively adsorb carbon dioxide due to its huge specific surface area and rich pore structure; organic membranes such as polyimide have good chemical stability and gas separation performance, but in actual applications, factors such as the membrane's pressure resistance, flux, and long-term stability need to be considered.

[0062] In one embodiment, the dust removal mechanism includes an electrostatic precipitator and a bag filter, the desulfurization mechanism includes a desulfurization tower and a spray pump, and the denitrification mechanism includes a denitrification reactor and a gas branch pipe provided on the denitrification reactor.

[0063] The combination of an electrostatic precipitator and a bag filter efficiently removes dust of different particle sizes. The electrostatic precipitator can effectively capture tiny dust particles and, utilizing the principle of charged deposition, achieves high dust removal efficiency for dust particles ranging from 0.01μm to 10μm. The bag filter finely filters larger dust particles, and pulse jet cleaning technology ensures that the bags always maintain excellent filtration performance, with extremely high filtration efficiency for dust particles larger than 0.5μm. Regarding desulfurization, limestone-gypsum wet desulfurization and ammonia-based desulfurization are available to meet different needs. Limestone-gypsum wet desulfurization utilizes limestone slurry to react with sulfur dioxide in the flue gas, converting it into gypsum. It has high desulfurization efficiency and a mature process. Ammonia-based desulfurization not only achieves efficient desulfurization, but also converts sulfur dioxide into valuable ammonium sulfate fertilizer raw material, thus achieving resource recycling. The denitrification mechanism utilizes selective catalytic reduction (SCR). Within a suitable temperature range, vanadium-titanium catalysts and other catalysts promote the reaction between ammonia and nitrogen oxides, reducing them to nitrogen and water, effectively reducing nitrogen oxide emissions. The coordinated operation of multiple purification mechanisms comprehensively enhances flue gas purification, reduces environmental pollution from harmful gases and dust, and provides a solid foundation for low-carbon emissions.

[0064] The electrostatic precipitator uses discharge and collection electrodes to charge dust and then deposit it, achieving a dust removal efficiency of over 99% for dust particles between 0.01μm and 10μm. The bag filter uses pulse jet cleaning to achieve a filtration efficiency of over 99.9% for dust particles larger than 0.5μm. The desulfurization structure adopts limestone-gypsum wet desulfurization or ammonia desulfurization. The limestone-gypsum wet desulfurization reacts limestone slurry with flue gas in an absorption tower, achieving a desulfurization efficiency of 95%-99%. The ammonia desulfurization uses ammonia solution to absorb sulfur dioxide to produce ammonium sulfate as a fertilizer raw material, achieving resource recycling and desulfurization efficiency of 90%-98%. The denitrification mechanism uses selective catalytic reduction to denitrify. At temperatures of 280°C to 420°C, ammonia reacts with nitrogen oxides using vanadium-titanium catalysts, achieving a denitrification efficiency of 80%-95%. Nitrogen oxides are reduced to nitrogen and water, effectively reducing nitrogen oxide emissions.

[0065] In one embodiment, the combustion device includes a low-nitrogen burner and a staged combustion structure connected to each other, and a plurality of fuel nozzles and air nozzles are staggeredly arranged on the combustion head of the low-nitrogen burner.

[0066] The combustion head of a low-NOx burner features staggered fuel and air nozzles, creating a separation between fuel-rich and fuel-lean zones. This arrangement creates a relatively oxygen-deficient environment during the initial combustion phase. The staggered arrangement of the fuel and air nozzles prevents the fuel from mixing adequately with air during this initial phase, creating a fuel-rich zone and suppressing the formation of thermal NOx. As combustion progresses, air is added to subsequent zones, forming a fuel-lean zone, reducing NOx formation by 30%-60%. This physical design spatially separates the fuel-rich and fuel-lean zones, ensuring the desired combustion reaction. Chronologically, combustion in the fuel-rich zone occurs in the early stages of combustion, while combustion in the fuel-lean zone occurs later. From a chemical reaction perspective, the fuel-rich zone is where incomplete combustion of the fuel occurs in the absence of oxygen. Reactions such as incomplete oxidation of carbon occur, producing intermediate products such as carbon monoxide. The fuel-lean zone, on the other hand, is where complete combustion occurs after air is added. Here, intermediate products such as carbon monoxide further react with oxygen to form carbon dioxide. By monitoring changes in gas composition during the combustion process, such as using gas sensors to detect the content of carbon monoxide, carbon dioxide, and oxygen in real time, it is possible to clearly distinguish between fuel-rich and fuel-lean zones. When the carbon monoxide content is high and the oxygen content is low, it can be determined that the combustion is in the fuel-rich zone; when the carbon monoxide content decreases, the carbon dioxide content increases significantly, and there is a certain amount of excess oxygen, it indicates that the fuel-lean zone combustion stage has begun. When the low-nitrogen burner is operating, in order to suppress the formation of thermal nitrogen oxides, the fuel-air ratio in the fuel-rich zone will deviate from the theoretical value, with relatively more fuel and less air. At this time, the mass ratio can reach 1:10-1:12. Air is added to the fuel-lean zone so that the final overall mixing ratio is close to the required range for complete combustion, to ensure full combustion of the fuel while reducing nitrogen oxide emissions.

[0067] The staged combustion structure divides the furnace into a lower main combustion zone and an upper burnout zone. 70%-80% of the theoretical air volume is introduced into the main combustion zone, creating a fuel-rich combustion area. The fuel-to-air mass ratio is higher than the theoretical complete combustion ratio, approximately 1:12-1:14. The remaining 20%-30% of air is introduced into the burnout zone to ensure that incomplete combustion is fully consumed. Ultimately, the fuel-to-air ratio throughout the combustion process reaches the optimal range for near-complete combustion, ensuring combustion efficiency and low pollutant emissions, ultimately reducing nitrogen oxide emissions by 20%-50%.

[0068] The unique staggered arrangement of fuel and air nozzles in the low-nitrogen burner allows the fuel to burn in an oxygen-deficient environment in the fuel-rich zone, fundamentally suppressing the generation of thermal nitrogen oxides. Air is then added to the fuel-lean zone to ensure complete combustion of the fuel, improving combustion efficiency while significantly reducing the generation of nitrogen oxides. The graded combustion structure rationally distributes the air volume to different areas of the furnace, forming a fuel-rich combustion zone in the main combustion zone, allowing the fuel to be fully preheated and initially burned, reducing the generation of nitrogen oxides. The remaining air is added to the burnout zone to ensure that incompletely burned substances are fully burned, further reducing nitrogen oxide emissions. The synergistic effect of these two technologies has significantly reduced the emission of nitrogen oxides, a major pollutant, which is conducive to improving the quality of the atmospheric environment and helping coal-fired power plants develop in a low-carbon and clean direction.

[0069] In one embodiment, the low-nitrogen burner and the staged combustion mechanism are both connected to a combustion parameter monitoring structure, and the combustion parameter monitoring structure is connected to the burner and the supporting gas supply device.

[0070] Both the low-nitrogen burner and the staged combustion structure are connected to a combustion parameter monitoring structure to monitor parameters such as combustion temperature, fuel and gas ratio in real time, and provide feedback to adjust the operation of the burner and gas supply device. This is because combustion temperature has a key impact on combustion efficiency and nitrogen oxide generation. When the combustion temperature is too high, it may cause a significant increase in nitrogen oxide generation. At this time, the monitoring structure will feedback signals to the burner and gas supply device to reduce the power of the burner or increase the gas supply to reduce the combustion temperature.

[0071] According to an embodiment of the present invention, on the other hand, a method for treating low-carbon emissions from a coal-fired power plant is provided, which uses a low-carbon emission system of a coal-fired power plant for treatment, and includes the following steps:

[0072] The pre-treated raw coal is mixed with the combustion-supporting gas and ignited to produce flue gas;

[0073] The flue gas is subjected to dust removal, desulfurization and denitrification treatment in sequence, while the composition of the flue gas after each treatment step is monitored, and the treatment parameters of the next step are adjusted according to the monitoring results;

[0074] Capture carbon dioxide from flue gas;

[0075] The captured carbon dioxide is reused or stored.

[0076] In one embodiment, when the amount of dust in the flue gas after dust removal exceeds the first predetermined value of desulfurization treatment, the spray flow rate is increased by 10%-20% or the concentration of the absorbent is increased by 5%-10%; when the sulfur dioxide content after desulfurization exceeds the second predetermined value of denitrification treatment, the injection amount of ammonia is increased by 5%-10% or the temperature is increased by 20°C.

[0077] If the dust content in the flue gas after dust removal is high and exceeds the design allowable value of the desulfurization mechanism (generally the dust content exceeds 50mg / m 3 It will have a significant impact on the desulfurization effect), which will cause slurry pollution in the absorption tower, clogging of nozzles and other problems, reducing the desulfurization efficiency. At this time, the desulfurization mechanism needs to be adjusted as follows: First, increase the spraying intensity and increase the flow rate of the slurry circulation pump to increase the amount of slurry sprayed into the absorption tower per unit time, enhance the washing effect of dust, and generally increase the flow rate by 10%-20%; second, increase the amount of absorbent. If limestone-gypsum wet desulfurization is used, the concentration of limestone slurry can be appropriately increased, usually from 20%-25% to 25%-30%, to replenish the absorbent consumed due to dust, to ensure the full progress of the desulfurization reaction. When the dust content in the flue gas after dust removal is within the normal range (generally less than 30mg / m 3 ), the desulfurization mechanism can maintain normal operating parameters, and only needs to monitor the dust content regularly to ensure that it remains stable at a normal level.

[0078] If the sulfur dioxide content in the flue gas after desulfurization exceeds the tolerance range of the denitrification mechanism (generally more than 100 mg / m 3 It will interfere with the denitration reaction), affect the activity of the denitration catalyst, and reduce the denitration efficiency. At this time, the denitration mechanism should make the following adjustments: on the one hand, increase the injection volume of ammonia. According to the excessive sulfur dioxide content, appropriately increase the injection volume of ammonia. Generally, for every 50mg / m 3 , the ammonia injection volume can be increased by 5%-10% to ensure sufficient ammonia to react with nitrogen oxides; on the other hand, the activity of the catalyst is optimized, and the temperature in the denitrification reactor is adjusted (appropriately increased within the range of 280℃-420℃, generally not exceeding 20℃ each time) to enhance the catalyst's tolerance to sulfur dioxide and promote the denitrification reaction. When the sulfur dioxide content of the flue gas after desulfurization is normal (generally less than 50mg / m 3 ), the denitrification mechanism operates according to normal procedures, and the catalyst activity is checked regularly to ensure stable denitrification efficiency.

[0079] The adjustment range of spray intensity is determined based on the flow field distribution, dust concentration and particle size in the desulfurization tower. Generally speaking, if the dust content exceeds the normal design value of 30mg / m 3 If the particle size is above 1μm-10μm, the spray intensity needs to be adjusted. Specifically, the spray intensity can be increased by increasing the flow rate of the desulfurization tower slurry circulation pump. Taking a common spray pump as an example, if the original flow rate is 500m 3 / h. When a high dust content is detected, the flow rate can be increased in stages, first increasing the flow rate by 10%, that is, increasing it to 550m 3 / h. After running for 1-2 hours, re-test the dust and sulfur dioxide concentrations at the inlet and outlet of the desulfurization tower. If the expected effect is still not achieved, it can be increased by 10%-15% again until the dust concentration drops significantly and the desulfurization efficiency stabilizes. However, the flow rate increase should generally not exceed 50% of the original flow rate to prevent excessive spraying volume from causing serious entrainment of mist in the tower, affecting the operation of subsequent equipment. Some desulfurization towers are equipped with multiple spray layers, and the number of layers to be opened can be determined according to the dust concentration. If the dust content is only slightly exceeded, only one layer of the spare spray layer can be opened; if the dust content exceeds the standard seriously, 2-3 layers can be opened. After opening a new spray layer, pay close attention to the pressure drop change in the tower to ensure that it is within the normal range (generally the pressure drop increase does not exceed 200Pa) to prevent it from affecting the stability of the desulfurization tower operation. Taking limestone-gypsum wet desulfurization as an example, the additional demand for absorbent is estimated based on the chemical reaction equation and the components in the dust that may react with the absorbent (such as metal oxides, etc.). Under normal circumstances, for every increase of 10mg / m 3 The theoretical amount of limestone (CaCO) needs to be increased by about 0.05kg / m 3 -0.1kg / m 3 Flue gas volume. When making actual adjustments, first add 80% of the theoretical increase to avoid waste and system blockage caused by excessive addition. In addition, the amount of absorbent can be increased by increasing the concentration of limestone slurry. If the original limestone slurry concentration is 20%, it can be gradually increased to 23%-25%. When increasing the concentration, use stirring equipment to ensure that the limestone particles are fully dispersed to prevent precipitation. At the same time, closely monitor the density and pH value of the slurry in the absorption tower. The slurry density is generally controlled at 1080kg / m 3 -1130kg / m 3 , the pH value is maintained at 5.0-5.8. If the density is too high or the pH value is out of range, it is necessary to appropriately reduce the amount of absorbent added or adjust other operating parameters.

[0080] If sulfur dioxide levels exceed the standard within the temperature range of 280°C-420°C, the temperature within the denitrification reactor can be appropriately increased to enhance catalyst activity. Generally, each temperature increase should be controlled within a range of 5°C-10°C. After the temperature is increased, the reactor should be allowed to stabilize for 1-2 hours to observe the denitrification efficiency and sulfur dioxide removal results. For example, if the current temperature is 320°C, the temperature can be initially increased to 325°C-330°C. However, it should be noted that excessively high temperatures may cause catalyst sintering and deactivation. Therefore, close monitoring of catalyst temperature changes is crucial. When the temperature approaches 420°C, temperature increases should be used with caution. If frequent temperature increases are used to maintain catalyst activity and the results are insufficient, catalyst regeneration should be considered. For vanadium-titanium catalysts, thermal regeneration and chemical regeneration can be used. Thermal regeneration is generally performed in an inert gas environment at 400°C-500°C to remove carbon deposits and some adsorbed impurities from the catalyst surface. Chemical regeneration involves soaking and cleaning the catalyst with specific chemical solutions (such as dilute sulfuric acid or sodium hydroxide solution) to restore its active sites. If the catalyst has been used for too long and its activity has significantly decreased, and even after multiple regenerations, it still cannot meet the requirements, it needs to be replaced. Some denitrification reactors use zoned ammonia injection. When sulfur dioxide levels exceed the standard in a certain area, the ammonia injection branch corresponding to the exceeded area can be adjusted specifically. By adjusting the valve on the branch, the ammonia injection rate in that area can be increased to ensure more complete contact and reaction between ammonia and nitrogen oxides and sulfur dioxide in the flue gas. During the adjustment process, attention should be paid to the uniformity of ammonia distribution in each area to avoid localized excessive ammonia slip. After adjusting the ammonia injection rate, continuously monitor the nitrogen oxide and sulfur dioxide concentrations at the denitrification reactor inlet and outlet, as well as the amount of ammonia slip. Based on the monitoring results, if nitrogen oxide and sulfur dioxide concentrations still do not meet the standards, the ammonia injection rate can be fine-tuned again. However, each adjustment should be limited to a minimum of 30% of the previous adjustment. At the same time, closely monitor ammonia slip. When ammonia slip exceeds 3 ppm, the ammonia injection rate should be increased cautiously to prevent adverse effects on the environment and equipment.

[0081] By increasing the spray flow rate, the amount of slurry sprayed into the absorption tower per unit time is increased, the dust washing effect is enhanced, and the concentration of the absorbent is increased to replenish the absorbent consumed by the influence of dust, ensuring the full progress of the desulfurization reaction; the ammonia injection volume is increased to ensure that there is enough ammonia to react with nitrogen oxides. Raising the temperature can optimize the activity of the catalyst, increase the catalyst's tolerance to sulfur dioxide, and promote the denitrification reaction.

[0082] In one embodiment, the combustion temperature of the raw coal and the supporting gas is 1300° C.-1400° C., the power adjustment range of the burner is 30%-100%, and the supply amount adjustment range of the supporting gas is 70%-150%.

[0083] Generally, when combustion temperatures exceed 1500°C, the production of thermal NOx increases significantly. To suppress NOx production, the combustion temperature must be controlled between 1300°C and 1400°C. When the temperature exceeds 1400°C, timely adjustment measures should be taken. When the temperature approaches 1300°C, it is important to prevent the temperature from dropping too low, which could lead to incomplete combustion and reduced efficiency. Common coal-fired power plant burners typically have a power adjustment range of 30% to 100%. When the combustion temperature is too high and adjustment is required, if the burner is currently operating at full load (100% power), the power can be gradually reduced based on actual conditions. For example, in some large power plants, the burner's full load power may be 50 MW. If the temperature is detected to be too high, the power can be initially reduced to around 80%, or 40 MW. If the temperature still does not decrease effectively, the power can be further reduced, but it is generally not recommended to drop below 30%, as excessively low power can lead to unstable combustion or even flameout. The adjustment of air supply is usually based on the theoretical air volume, and the adjustment range is generally between 70% and 150%. When the combustion temperature is too high, the air supply will be increased. Assuming that the theoretical air supply of a burner is 10,000m 3 / h. When cooling is required, the air supply can be increased by 20%, that is, to 12000m 3 / h. If the temperature drop effect is not obvious, the air supply can be increased, but generally not more than 50% of the theoretical air volume, that is, not more than 15000m 3 On the contrary, if the temperature drops too fast or the combustion is abnormal during the adjustment process, the air supply can be appropriately reduced, but the reduction should generally not exceed 30%, that is, not less than 7000m 3 / h to ensure the stability and completeness of combustion.

[0084] Within this combustion temperature range, the coal can be fully burned to maintain the power generation efficiency of the power plant, and the generation of thermal nitrogen oxides can be effectively reduced; the supply adjustment range of the supporting combustion gas ensures the stability and sufficiency of the combustion.

[0085] Although the embodiments of the present invention have been described with reference to the accompanying drawings, those skilled in the art may make various modifications and variations without departing from the spirit and scope of the present invention. Such modifications and variations are all within the scope defined by the appended claims.

Claims

1. A low-carbon emission system for coal-fired power plants, characterized in that: include: Pre-processing device, suitable for pre-processing raw coal and then transporting it to the next process; A combustion device, connected to the pre-treatment device, suitable for mixing raw coal and supporting gas and then performing combustion treatment; A flue gas purification device comprising a dust removal mechanism, a desulfurization mechanism, and a denitrification mechanism connected in sequence, wherein the dust removal mechanism is connected to the combustion device, and a flue gas composition monitoring mechanism is provided between the dust removal mechanism and the desulfurization mechanism, and between the desulfurization mechanism and the denitrification mechanism, respectively. The flue gas composition monitoring mechanism is adapted to monitor operating parameters of the dust removal mechanism and the desulfurization mechanism and transmit the information to a controller, which adjusts the operating parameters of the desulfurization mechanism and the denitrification mechanism according to the monitoring results. a carbon dioxide capture device connected to the denitrification mechanism and adapted to capture carbon dioxide in the flue gas output by the denitrification mechanism; The carbon dioxide utilization and storage device is connected to the carbon dioxide capture device and is suitable for reusing or storing the carbon dioxide captured by the carbon dioxide capture device.

2. The low-carbon emission system for coal-fired power plants according to claim 1, characterized in that: The carbon dioxide utilization and storage device includes a seismic monitor, a water quality sensor, a flow monitor, a carbon dioxide delivery pipeline, and a pressure and flow stabilizing structure arranged on the carbon dioxide delivery pipeline.

3. The low-carbon emission system for coal-fired power plants according to claim 1, characterized in that: The carbon dioxide capture device includes a chemical absorption structure, a physical adsorption structure and a membrane separation structure. Switching valves are provided between the chemical absorption structure, the physical adsorption structure and the membrane separation structure, and the switching valves are all connected to the controller signal.

4. The low-carbon emission system for coal-fired power plants according to claim 3, characterized in that: The chemical absorption structure includes an absorption tower and a regeneration tower, the physical adsorption structure is activated carbon, and the membrane separation structure is a polyimide membrane.

5. The low-carbon emission system for coal-fired power plants according to any one of claims 1 to 4, characterized in that: The dust removal mechanism includes an electrostatic precipitator and a bag dust collector, the desulfurization mechanism includes a desulfurization tower and a spray pump, and the denitrification mechanism includes a denitrification reactor and a gas branch pipe arranged on the denitrification reactor.

6. The low-carbon emission system for coal-fired power plants according to any one of claims 1 to 4, characterized in that: The combustion device comprises a low-nitrogen burner and a staged combustion structure that are connected to each other. A plurality of fuel nozzles and air nozzles are staggeredly arranged on the combustion head of the low-nitrogen burner.

7. The low-carbon emission system for coal-fired power plants according to claim 6, characterized in that: The low-nitrogen burner and the staged combustion mechanism are both connected to a combustion parameter monitoring structure, and the combustion parameter monitoring structure is connected to the burner and the supporting gas supply device.

8. A method for treating low-carbon emissions from coal-fired power plants, characterized in that: The method of using the low-carbon emission system for coal-fired power plants according to any one of claims 1 to 7 for treatment comprises the following steps: The pre-treated raw coal is mixed with the combustion-supporting gas and ignited to produce flue gas; The flue gas is subjected to dust removal, desulfurization and denitrification treatment in sequence, while the composition of the flue gas after each treatment step is monitored, and the treatment parameters of the next step are adjusted according to the monitoring results; Capture carbon dioxide from flue gas; The captured carbon dioxide is reused or stored.

9. The method for treating low-carbon emissions from coal-fired power plants according to claim 8, characterized in that: When the amount of dust in the flue gas after dust removal exceeds the first predetermined value of desulfurization treatment, increase the spray flow rate by 10%-20% or increase the concentration of the absorbent by 5%-10%; when the sulfur dioxide content after desulfurization exceeds the second predetermined value of denitrification treatment, increase the ammonia injection amount by 5%-10% or increase the temperature by 20°C.

10. The method for treating low-carbon emissions from coal-fired power plants according to claim 9, characterized in that: The combustion temperature of the raw coal and the supporting gas is 1300°C-1400°C, the power adjustment range of the burner is 30%-100%, and the supply adjustment range of the supporting gas is 70%-150%.

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