A burner for producing high hydrogen using low-slurrying coal quality and its control method

Abstract

The present application provides a burner for producing high hydrogen from low-slurry-forming coal quality, including a burner central tube (start-up burner passage), a first burner outer tube, a second burner outer tube, a first pipeline outlet collecting nozzle, a first burner outer tube nozzle, a second burner outer tube nozzle and a cooling jacket which are coaxially nested and connected. The first burner outer tube is nested outside the burner central tube to form a first outer ring channel; the second burner outer tube is nested outside the first burner outer tube to form a second outer ring channel; a plurality of first pipelines and second pipelines are uniformly distributed in the second outer ring channel. The present application can effectively control the vertical temperature field of the gasifier wall, ensure that the gasifier wall does not exceed the temperature under different loads, and the slag outlet does not block slag. The present application solves the problems of the existing gasifier burner, such as harsh requirements for coal quality, low hydrogen production, low service life and poor safety.

Description

Technical Field

[0001] The present application relates to the technical field of coal chemical engineering, and particularly relates to a burner for producing high hydrogen from low-slurry-forming coal quality and a control method thereof. Background Art

[0002] In the clean and efficient utilization of coal, coal gasification technology plays a core role. The dry pulverized coal pressurized entrained flow gasification technology is widely used because of its advantages such as wide coal type adaptability, high gasification efficiency, and excellent environmental protection performance. At present, for most of the dry pulverized coal gasification technologies, the slagging and residence time of most gasifiers are designed according to the concepts such as the burner injection angle and the height-diameter ratio of the gasifier, especially for the gasifiers using high-ash, high-sulfur, and high-ash fusion point coal as raw materials. In order to pursue a higher carbon conversion rate, the larger the height-diameter ratio of the gasifier, the more obvious the over-temperature of the gasifier arch top and the blockage and protrusion of the lower slag outlet caused by the increase and decrease of the load. The higher the load, the more easily the furnace wall is eroded by high-temperature media and ablated, and the more difficult it is to slag, there is a risk of burning out the gasification water-cooled wall. The lower the load, the more easily the slag outlet is blocked. At the same time, for the gasifier with multiple side-mounted burners, the same problem also exists. To ensure smooth slag discharge and increase the operation temperature of the gasifier, the effective gas of the gasifier is relatively low, and the gasifier arch top is prone to over-temperature. At the same time, the slag pulling of the gasifier is easy to block the downstream channel. To prevent the over-temperature of the gasifier arch top, when operating at a lower furnace temperature, the slag outlet is easy to block.

[0003] In the existing dry pulverized coal gasification technology, due to the low water content in the pulverized coal entering the furnace, the hydrogen content in the produced syngas is relatively low, which cannot meet the synthesis requirements of downstream devices with high hydrogen content (such as ammonia synthesis devices). For some gasification technologies, high-quality steam is selected to be added to the gasification burner, resulting in large energy consumption, but the hydrogen content in the syngas only increases slightly and cannot meet the requirements of downstream devices. If the existing dry pulverized coal gasification technology is adopted, the conversion capacity of the conversion device needs to be increased, resulting in a significant increase in energy consumption.

[0004] In the existing water coal slurry gasification technology, the hydrogen content in the produced syngas is relatively higher than that of the traditional dry pulverized coal gasification technology. However, the water coal slurry gasification process has strict requirements on coal quality. For coals with an internal water content higher than 8% and high coal quality metamorphism degree, the slurry-forming property is very poor, the gasification efficiency is low, and at the same time, the existing water coal slurry gasification process has a low carbon conversion rate and a low service life of the burner. Summary of the Invention

[0005] The present application provides a burner for producing high hydrogen from low-slurry-forming coal quality and a control method thereof to solve the problems of the existing burner, such as strict requirements on coal quality, low hydrogen production, low service life, and poor safety.

[0006] The present application provides a burner for producing high hydrogen from low-slurry-forming coal quality, including:

[0007] The burner central pipe, the first burner outer pipe, the second burner outer pipe, the first pipeline outlet collecting nozzle, the first burner outer pipe nozzle, the second burner outer pipe nozzle and the cooling jacket which are coaxially nested and connected;

[0008] The first burner outer pipe is nested outside the burner central pipe to form a first outer ring channel;

[0009] The second burner outer pipe is nested outside the first burner outer pipe to form a second outer ring channel;

[0010] The cooling jacket is arranged on the outside of the second burner outer pipe;

[0011] A number of first pipeline outlet collecting nozzles are evenly distributed in the second outer ring channel. The first burner outer pipe nozzle and the second burner outer pipe nozzle are respectively a truncated cone pipe, and the inner contraction angle is between 0 - 40°;

[0012] A number of first pipelines are evenly distributed in the second outer ring channel, and the first pipelines are arranged in a rotating tangential layout;

[0013] A number of second pipelines are evenly distributed in the second outer ring channel, and the second pipelines are arranged in a rotating tangential layout;

[0014] An annular partition is arranged between the first pipelines and the second pipelines.

[0015] The first outer ring channel is provided with a swirler, and 0 - 2000 mm in front of the swirler, the first outer ring channel is set as a bypass channel, and the outer diameter of the swirler is the same as the inner diameter of the first outer ring channel;

[0016] The swirler includes a number of swirl vanes.

[0017] Gas / protective gas and ignition oxygen enter the gasifier through the burner central pipe;

[0018] Main oxygen enters the gasifier through the first outer ring channel;

[0019] Pulverized coal enters the gasifier through the first pipelines;

[0020] Waste liquid or protective gas enters the gasifier through the second pipelines, and the waste liquid is waste water containing macromolecular organic substances, toxic and harmful substances, etc.

[0021] The pipe diameter range of the first pipelines is φ30 - 60.

[0022] The pipe diameter range of the second pipelines is φ20 - 40.

[0023] Each of the first pipelines is provided with an independent control valve respectively, and each of the second pipelines is provided with an independent control valve respectively. Each pipeline can control the waste liquid and the protective gas separately, or can control the waste liquid and the protective gas simultaneously.

[0024] The end of the second pipeline is in a rotary tangential layout.

[0025] The inner inclination angle of the outer pipe nozzle of the second burner is smaller than that of the outer pipe nozzle of the first burner.

[0026] In a second aspect, the present application provides a control method for a burner that uses low-slurry-forming coal quality to produce high hydrogen, which is applied to the burner and includes:

[0027] Inject fuel gas / protective gas and oxygen into the central pipe of the burner;

[0028] Perform an ignition operation on the oxygen and the fuel gas;

[0029] Gradually increase the flow rates of the fuel gas and oxygen, and detect the first-stage parameters in the gasifier at this time. The first-stage parameters include temperature and pressure;

[0030] When the first-stage parameters reach the preset threshold, and protective gas is introduced into the first outer ring channel, the first pipeline, and the second pipeline;

[0031] Inject pulverized coal into the first pipeline and inject oxygen into the first outer ring channel to perform the coal feeding operation;

[0032] Inject oxygen, fuel gas or protective gas into the central pipe of the burner to obtain the second-stage parameters in the gasifier at this time. The second-stage parameters include load, water wall heat flux, gas composition, and slag notch differential pressure;

[0033] According to the second-stage parameters, gradually withdraw the protective gas in the second pipeline, and gradually introduce waste liquid into the second pipeline. When the load of the gasifier is low, the waste liquid and the protective gas in the second pipeline are used in combination. The waste liquid is waste water containing macromolecular organic substances, toxic and harmful substances, etc.

[0034] The flow rate of the waste liquid in the second pipeline is adjusted in real time according to the second-stage parameters.

[0035] As can be seen from the above technical solutions, the present application provides a burner for producing high hydrogen using low-slurry-forming coal quality, including a burner central tube, a first burner outer tube, a second burner outer tube, a first pipeline outlet collecting nozzle, a first burner outer tube nozzle, a second burner outer tube nozzle, and a cooling jacket that are coaxially nested and connected. The second burner outer tube is nested outside the first burner outer tube to form a second outer ring channel. A plurality of first pipelines and second pipelines are uniformly distributed in the second outer ring channel. An annular partition is arranged between the first pipeline and the second pipeline. A swirler is provided in the first outer ring channel, and at a position 0 - 2000 mm in front of the swirler, the oxygen channel is set as a bypass channel. The present application can effectively control the vertical temperature field of the gasifier wall. By accurately controlling the flow rate of each pipeline according to the parameters in the gasifier, it is ensured that the wall of the gasifier does not exceed the temperature and the slag outlet is not blocked with slag under different loads. The present application solves the problems of the existing gasifier burner being demanding on coal quality, having low hydrogen production, low service life, and poor safety. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] In order to more clearly illustrate the technical solutions of the present application, the drawings required for use in the embodiments will be briefly introduced below. Obviously, for those of ordinary skill in the art, other drawings can also be obtained based on these drawings without creative efforts.

[0037] Figure 1 It is a schematic structural diagram of a burner for producing high hydrogen using low-slurry-forming coal quality according to the present application. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0038] The embodiments will be described in detail below, and the examples are shown in the drawings. When the following description refers to the drawings, unless otherwise indicated, the same numbers in different drawings represent the same or similar elements. The embodiments described in the following examples do not represent all embodiments consistent with the present application. They are only examples of systems and methods consistent with some aspects of the present application detailed in the claims.

[0039] See Figure 1 , the present application provides a burner for producing high hydrogen using low-slurry-forming coal quality, including:

[0040] A burner central tube 1, a first burner outer tube 2, a second burner outer tube 3, a first pipeline outlet collecting nozzle 4, a first burner outer tube nozzle 5, a second burner outer tube nozzle 6, and a cooling jacket 7 that are coaxially nested and connected;

[0041] The first burner outer tube 2 is nested outside the burner central tube 1 to form a first outer ring channel 8;

[0042] The second burner outer tube 3 is nested outside the first burner outer tube 2 to form a second outer ring channel 9;

[0043] The cooling jacket 7 is arranged outside the outer tube 3 of the second burner.

[0044] The collecting nozzle 4 at the outlet of the first pipeline, the nozzle 5 of the outer tube of the first burner, and the nozzle 6 of the outer tube of the second burner are respectively a truncated conical tube.

[0045] A plurality of first pipelines 10 are evenly distributed in the second outer ring channel 9, and the first pipelines 10 are arranged in a rotating tangential layout; more specifically, the ends of the first pipelines 10 are arranged in a rotating tangential layout, which can effectively ensure that the pulverized coal uniformly swirls out from the annular channel, uniformly mixes with oxygen, and improves the gas production rate.

[0046] A plurality of second pipelines 11 are evenly distributed in the second outer ring channel 9, and the second pipelines 11 are arranged in a rotating tangential layout; more specifically, the ends of the second pipelines 11 are arranged in a rotating tangential layout, which can effectively ensure that the waste liquid uniformly swirls out from the annular channel, uniformly mixes with the syngas produced by the combustion of pulverized coal and oxygen, and undergoes a secondary reaction, improving the hydrogen production efficiency and ensuring the temperature of the gasifier furnace wall at the same time.

[0047] An annular partition 12 is arranged between the first pipeline 10 and the second pipeline 11.

[0048] More specifically, the annular partition 12 is used to separate the pulverized coal outlet in the first pipeline 10 from the waste liquid outlet in the second pipeline 11, and the waste water pipe branches in the annular channel outside the partition continue to extend forward to prevent the pulverized coal from mixing with the waste liquid and affecting the normal production.

[0049] The first outer ring channel 8 is provided with a swirler 13, and the outer diameter of the swirler 13 is the same as the inner diameter of the first outer ring channel 8; more specifically, in order to ensure the swirl intensity, at 0 - 2000 mm in front of the swirler, the first outer ring channel 8 is set as a bypass channel, and by using the swirler, a strong swirl can be provided for oxygen, effectively improving the mixing degree of pulverized coal and oxygen and the gas production rate. After the second pipeline 11 is put into use, even if low-slurrying pulverized coal is used as the raw material, a high hydrogen production rate can still be ensured.

[0050] The swirler 13 includes a plurality of swirl vanes.

[0051] Gas / protective gas or oxygen enters the gasifier through the central tube 1 of the burner.

[0052] Main oxygen enters the gasifier through the first outer ring channel 8.

[0053] More specifically, the oxygen adopts a single-branch multi-channel layout to control the oxygen flow rate as a whole.

[0054] Pulverized coal enters the gasifier through the first pipeline 10;

[0055] The waste liquid enters the gasifier through the second pipeline 11, and the waste liquid is waste water containing macromolecular organic substances, toxic and harmful substances, etc.

[0056] The pipe diameter range of the first pipeline 10 is φ30 - 60.

[0057] The pipe diameter range of the second pipeline 11 is φ20 - 40.

[0058] Each of the first pipelines 10 is provided with an independent control valve, and each of the second pipelines 11 is provided with an independent control valve, and each pipeline can control the waste liquid and the protective gas separately, or can control the waste liquid and the protective gas simultaneously.

[0059] More specifically, by independently controlling the pulverized coal in multiple first pipelines 10 through independent control valves, the flow rate of the pulverized coal can be effectively controlled, and the reaction can be precisely controlled. The waste liquid in the second pipeline 11 is also precisely controlled through independent control valves. In some embodiments, every 1 - 2 second pipelines 11 are controlled by one control valve for the flow rate of the waste liquid therein, and the number of the second pipelines 11 controlled by the control valve can be adjusted in real time according to the actual situation.

[0060] The end of the second pipeline 11 is arranged in a rotating tangential layout. More specifically, setting the end of the second pipeline 11 in a rotating tangential layout can effectively ensure that the waste liquid evenly swirls out from the annular channel, uniformly mixes with the synthesis gas produced by the combustion of pulverized coal and oxygen for a secondary reaction, improves the hydrogen production efficiency, and at the same time, the waste liquid vaporizes and absorbs heat to reduce the temperature of the high-temperature synthesis gas and ensure the temperature of the gasifier furnace wall.

[0061] The inner inclination angle of the outer pipe nozzle 6 of the second burner is smaller than that of the outer pipe nozzle 5 of the first burner. More specifically, it ensures that the pulverized coal contacts and mixes with oxygen inward, burns fully, improves the carbon conversion rate, and further increases the output of effective gas; it can effectively control the vertical temperature field of the gasifier under different loads, and ensure the slagging stability of the gasifier and the smoothness of the slag discharge port.

[0062] In a second aspect, the present application provides a control method for a burner that uses low-slurry-forming coal quality to produce high hydrogen, which is applied to the burner, and includes the following steps:

[0063] Inject fuel gas / protective gas and oxygen into the central pipe 1 of the burner;

[0064] More specifically, the burner is arranged in the combustion chamber area, and the combustion chamber area is provided with a flame monitoring facility, an ignition device, and a start-up burner. The ignition burner has functions of start-up ignition, heating up and pressurizing, assisting in pressure relief, slightly adjusting the combustion flow field of the gasifier, igniting pulverized coal and online ignition, heat preservation, and pressure maintenance.

[0065] Carry out an ignition operation on the oxygen and the fuel gas;

[0066] More specifically, at this time, the pressure range inside the gasifier is 0.2 - 0.7 MPa, and the inside of the gasifier is in an inert condition at this time, which can ensure the safe and normal progress of the ignition operation, avoid affecting production, improve production efficiency, and further improve economic benefits.

[0067] More specifically, when the first gasifier of the device is started up, fuel gas needs to be introduced from outside the battery limit. Therefore, fuel gas and oxygen need to be introduced into the inner part of the burner central pipe 1. After successful ignition, after purified gas is generated inside the system, the purified gas generated by the reaction is used for the ignition operation.

[0068] Gradually increase the flow rates of the fuel gas and oxygen, and detect the first-stage parameters inside the gasifier at this time. The first-stage parameters include temperature and pressure;

[0069] When the first-stage parameters reach the preset threshold values, and protective gas is introduced into the first outer ring channel 8, the first pipeline 10, and the second pipeline 11;

[0070] Inject pulverized coal into the first pipeline 10, and inject oxygen into the first outer ring channel 8 to carry out the coal feeding operation;

[0071] Introduce fuel gas, oxygen, or protective gas into the burner central pipe 1 to obtain the second-stage parameters inside the gasifier at this time. The second-stage parameters include load, water wall heat flux, gas composition, and slag notch differential pressure;

[0072] According to the second-stage parameters, gradually withdraw the protective gas in the second pipeline 11, and gradually introduce waste liquid into the second pipeline 11. When the load of the gasifier is low, the waste liquid and the protective gas can be used in combination. The waste liquid is waste water containing macromolecular organic substances, toxic and harmful substances, etc.

[0073] The flow rate of the waste liquid in the second pipeline 11 is adjusted in real time according to the second-stage parameters.

[0074] More specifically, the amount of waste liquid input reaches 20%-40% of the total input amount, and the total input amount is the sum of the input amounts of waste liquid and pulverized coal. Since a large amount of waste liquid enters the gasifier through the second pipeline 11, a large amount of water vapor is generated in the gasification chamber. A partial CO shift reaction will occur in the gasifier, and a relatively large amount of CO will be converted into CO2, while obtaining the product H2 with the same molar mass. At high temperatures, the reaction rate of the shift reaction is very high, so that the hydrogen content in the effective gas of the gasification reaction reaches 34%-38% of the hydrogen content in the water slurry gasification. At the same time, the water content in the raw gas leaving the gasifier is relatively large, and this part of the vapor has been heated to about 1400 °C by the combustion of pulverized coal and oxygen. After quenching, the water content in the raw gas is relatively large, and the steam-gas ratio at the outlet of the scrubbing tower reaches the water slurry gasification quenching technology, and the production efficiency is about 30% higher than that of the traditional dry pulverized coal gasification quenching technology. The downstream device conversion does not need to add steam again to meet the downstream synthesis demand with a high hydrogen content, such as a synthetic ammonia device. Moreover, this part of the heat is by-produced as steam in the conversion section. Using the burner of the present application reduces the investment and energy consumption of the downstream conversion device. The oxygen increased by the added wastewater is reflected in the form of steam in the conversion section. If a waste heat boiler process is adopted, the oxygen increased by the added wastewater is recovered as high-quality steam in the waste heat boiler section.

[0075] Compared with the prior art, the method provided by the present application can effectively control the vertical temperature field of the gasifier, ensuring that the furnace wall does not overheat and the slag notch does not block slag under different loads of the gasifier. The on-line operation safety and long-term operation of the gasification device are significantly improved as a whole; the effective gas production rate is high, and the hydrogen content in the effective gas is high; the adaptability to coal is strong, meeting the needs of downstream high-hydrogen-content devices under coal quality changes; the proportion of waste water co-firing is large, and the service life of the burner is long, etc. Many advantages, thereby improving the safety, stability and economy of the gasifier operation, ensuring the on-line operation rate of the device, and reducing the production cost per unit product.

[0076] As can be seen from the above technical solutions, the present application provides a burner for producing high hydrogen using low-slurrying coal quality, including a burner central tube 1, a first burner outer tube 2, a second burner outer tube 3 connected in coaxial nesting, a plurality of first pipeline outlet collecting nozzles 4, a first burner outer tube nozzle 5, a second burner outer tube nozzle 6 and a cooling jacket 7 uniformly distributed in the second outer ring channel. The first burner outer tube 2 is nested outside the burner central tube 1 to form a first outer ring channel 8, the second burner outer tube 3 is nested outside the first burner outer tube 2 to form a second outer ring channel 9, the cooling jacket 7 is arranged outside the second burner outer tube 3, and the first pipeline outlet collecting nozzle 4, the first burner outer tube nozzle 5 and the second burner outer tube nozzle 6 are respectively a truncated cone tube; a plurality of first pipelines 10 are uniformly distributed in the second outer ring channel 9, the first pipelines 10 are arranged in a rotating tangential layout, a plurality of second pipelines 11 are uniformly distributed in the second outer ring channel 9, and the second pipelines 11 are arranged in a rotating tangential layout. An annular partition 12 is arranged between the first pipelines 10 and the second pipelines 11. The present application can effectively control the vertical temperature field of the gasifier wall. By accurately controlling the flow rate of each pipeline according to the parameters in the gasifier, it is ensured that the wall of the gasifier does not exceed the temperature and the slag outlet is not blocked with slag under different loads. The present application solves the problems of the existing gasifier burner being demanding on coal quality, having low hydrogen production, low service life and poor safety.

[0077] For the similar parts between the embodiments provided in the present application, reference can be made to each other. The specific embodiments provided above are only several examples under the general concept of the present application and do not constitute a limitation on the protection scope of the present application. For those skilled in the art, any other embodiments extended based on the solution of the present application without creative efforts belong to the protection scope of the present application.

Claims

1. A burner for producing high hydrogen using low-slurrying coal quality, characterized in that, Comprising: A burner central tube (1), a first burner outer tube (2), a second burner outer tube (3), a first pipeline outlet collecting nozzle (4), a first burner outer tube nozzle (5), a second burner outer tube nozzle (6), and a cooling jacket (7) which are coaxially nested and connected; the burner central tube (1) is an ignition burner passageway; The first burner outer tube (2) is nested outside the burner central tube (1) to form a first outer ring passageway (8); The first outer ring passageway (8) is provided with a swirler (13), and at a position 0 - 2000 mm in front of the swirler, the passageway of the first outer ring passageway (8) is set as a bypass passageway, and the outer diameter of the swirler (13) is the same as the inner diameter of the first outer ring passageway (8); The swirler (13) comprises a plurality of swirl vanes; The second burner outer tube (3) is nested outside the first burner outer tube (2) to form a second outer ring passageway (9); The cooling jacket (7) is arranged outside the second burner outer tube (3); A plurality of first pipeline outlet collecting nozzles (4), first burner outer tube nozzles (5), and second burner outer tube nozzles (6) are evenly distributed in the second outer ring passageway (9); the first pipeline outlet collecting nozzle (4), the first burner outer tube nozzle (5), and the second burner outer tube nozzle (6) are respectively truncated cone tubes, and the inner contraction angle is between 0 - 40°; the inner inclination angle of the second burner outer tube nozzle (6) is smaller than that of the first burner outer tube nozzle (5); A plurality of first pipelines (10) are evenly distributed in the second outer ring passageway (9), and the first pipelines (10) are arranged in a rotating tangential layout; A plurality of second pipelines (11) are evenly distributed in the second outer ring passageway (9), and the second pipelines (11) are arranged in a rotating tangential layout; Each of the first pipelines (10) is provided with an independent control valve, each of the second pipelines (11) is provided with an independent control valve, and each pipeline can control waste liquid and protective gas separately, or can control waste liquid and protective gas simultaneously; An annular partition (12) is arranged between the first pipelines (10) and the second pipelines (11); Fuel gas or protective gas and ignition oxygen enter the gasifier through the burner central tube (1); Main oxygen enters the gasifier through the first outer ring passageway (8); Pulverized coal enters the gasifier through the first pipeline (10); Waste liquid or protective gas enters the gasifier through the second pipeline (11), and the waste liquid is toxic and harmful wastewater containing macromolecular organic substances.

2. The burner for producing high hydrogen using low-slurrying coal quality according to claim 1, characterized in that, The pipe diameter range of the first pipeline (10) is φ30 - 60.

3. The burner for producing high hydrogen using low-slurrying coal quality according to claim 1, characterized in that, The pipe diameter range of the second pipeline (11) is φ20 - 40.

4. The burner for producing high hydrogen using low-slurrying coal quality according to claim 1, characterized in that, The end of the second pipeline (10) is arranged in a rotating tangential layout, and the outlet inclination angle is 0 - 40°; the end of the second pipeline (11) is arranged in a rotating tangential layout, and the outlet inclination angle is 0 - 40°.

5. A control method for a burner for producing high hydrogen using low-slurrying coal quality, applied to the burner according to any one of claims 1-4, characterized in that, Including the following steps: Introduce fuel gas / protective gas and oxygen into the burner central tube (1), and conduct an ignition operation on the oxygen and the fuel gas; Gradually increase the flow rates of the fuel gas and oxygen, and detect the first-stage parameters in the gasifier at this time, and the first-stage parameters include temperature and pressure; When the parameters in the first stage reach the preset threshold, and protective gas is introduced into the first outer ring channel (8), the first pipeline (10), and the second pipeline (11); Pulverized coal is introduced into the first pipeline (10), and oxygen is introduced into the first outer ring channel (8) for coal feeding operation; Fuel gas, oxygen, or protective gas is introduced into the burner central pipe (1) to obtain the second-stage parameters in the gasifier at this time. The second-stage parameters include load, water wall heat flux, gas composition, and slag notch differential pressure; According to the second-stage parameters, the protective gas in the second pipeline (11) is gradually withdrawn, and waste liquid is gradually introduced into the second pipeline (11). The waste liquid is waste water containing macromolecular organic substances and toxic and harmful substances.

6. The control method for a burner for producing high hydrogen using low-slurrying coal quality according to claim 5, characterized in that, The flow rate of the waste liquid in the second pipeline (11) is adjusted in real time according to the second-stage parameters.

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