A test system and testing method for simulating different flue gas environments

Abstract

The present invention discloses a test system and a test method for simulating different flue gas environments. The test system can generate the main components such as gas components, solid dust particles, and vapors in the test flue gas. The reaction furnace can provide the denitrification reaction conditions, and the heating temperature required for simulating the desulfurization and wet electrostatic environment can be simulated in the pipeline system. The gas after the reaction in the reaction furnace is introduced into the pipeline system. The flue gas parameters in the pipeline can be detected by the detection components arranged on the pipeline system, and then the flow rates of the gas components, solid dust particles, and vapors can be adjusted, so as to obtain the simulated flue gas that meets the test requirements. The test personnel only need to sample and analyze the flue gas in the pipeline without on-site sampling, which not only improves the sampling efficiency, but also can simulate the flue gas under different conditions by changing the parameters in the test system, improves the sampling flexibility, and the sampling is less affected by the environment, increasing the accuracy of the later test research.

Description

Technical Field

[0001] The present invention relates to the technical field of flue gas treatment, and particularly to a test system for simulating different flue gas environments and different test studies conducted on the test system, such as SO3 sampling, denitrification, and physical and chemical property testing methods. Background Art

[0002] At present, coal-fired power plants are gradually improving towards environmental protection, cleanliness, and energy conservation, and there are increasingly high standards for flue gas emissions. How to achieve "ultra-clean emissions" has become a research hotspot. Correspondingly, in the environmental protection equipment at the tail of coal-fired boilers and their connecting flue ducts, problems such as equipment corrosion, air preheater blockage, and the accuracy of coal-fired flue gas sampling and testing methods have gradually become the key concerns of experimental personnel in this field.

[0003] For example: First, inside SCR denitrification, due to the high flue gas temperature, corrosive gases in the flue gas mainly exist in gaseous form, and the internal corrosion of denitrification equipment is relatively less obvious. However, SCR denitrification catalysts often contain active components such as V2O5, and V2O5 can promote the catalytic oxidation of flue gas SO2 to generate SO3. Flue gas SO3 can trigger the corrosion risk of downstream environmental protection equipment. Therefore, when selecting a suitable catalyst for SCR denitrification, it is necessary to ensure both the improvement of denitrification catalytic efficiency and the inhibition of the catalytic oxidation of flue gas SO2 to generate SO3. Second, in the air preheater, the flue gas temperature is reduced. Since flue gas SO3 is extremely easy to combine with water vapor to form SO3 / H2SO4, and due to the existence of a certain amount of escaped NH3 in SCR denitrification, the generated H2SO4 can react with the escaped NH3 to form ammonium sulfate or ammonium bisulfate (ABS). In the temperature range of the air preheater, ammonium bisulfate is in the stage of changing from liquid to solid, with extremely strong adsorption, and it is very easy to adsorb on dust, increasing the viscosity of the dust, thereby causing blockage of the air preheater. Third, in SCR flue gas denitrification equipment, the high-temperature flue gas environment is extremely likely to damage the sampling pipeline, posing higher requirements for the sampling and testing systems of NH3 escape, flue gas NO, SO2, and SO3. In wet flue gas desulfurization or wet electrostatic precipitators, due to the low internal flue gas temperature, low dust concentration, and high moisture content, there are many influencing factors for flue gas SO3 sampling and testing, and correspondingly, higher requirements are put forward for the accuracy of flue gas SO3 sampling and testing, etc.

[0004] Currently, for the problems related to the above environmental protection equipment, we mainly adjust the operating parameters of the environmental protection equipment at the coal-fired power plant site and conduct corresponding performance tests. Through sampling and testing cases under different operating conditions of multiple power plants, we draw experience, actively explore, and continuously improve the existing sampling and testing methods, and use the test data to guide and optimize the on-site operation management.

[0005] However, on-site testing is troublesome, the testing cycle is long, and there are factors such as the instability of on-site working conditions.

[0006] In view of this, how to shorten the testing cycle and improve the testing accuracy is an urgent problem to be solved by those skilled in the art. Summary of the Invention

[0007] To solve the above technical problems, the present invention provides a test system for simulating different flue gas environments, including the following components:

[0008] A flue gas generation system for generating the gas components in the test flue gas;

[0009] A feeding and generating system for generating solid dust particles in the test flue gas;

[0010] A vapor generation system for generating vapor in the test flue gas;

[0011] A reaction furnace, including a furnace body forming a cavity, the furnace body is provided with a gas inlet and a gas outlet communicating with the cavity, and the gas inlet is used to communicate with the outlet of the flue gas generation system; an installation structure for storing the denitration catalyst is also provided in the cavity; the reaction furnace further includes a temperature control device for heating the cavity to heat the cavity of the reaction furnace;

[0012] A pipeline system is arranged downstream of the reaction furnace, its inlet communicates with the gas outlet of the reaction furnace, the outlets of the feeding and generating system and the vapor generation system are both communicated with the pipeline system, and a detection component is arranged on the pipe wall of the pipeline system for detecting the flue gas parameters in the pipeline.

[0013] The test system provided by the present invention can generate the main components such as gas components, solid dust particles, and vapor in the test flue gas. The temperature control device can heat the cavity of the reaction furnace, so as to provide the actual temperature required for the denitration reaction and the heating temperature required for simulating the desulfurization and wet electrostatic environment in the subsequent pipeline system. The reacted gas is introduced into the pipeline system, and the flue gas parameters in the pipeline can be detected by the detection component arranged on the pipeline system, and then the flow rates of the gas components, solid dust particles, and vapor can be adjusted, so as to obtain the simulated flue gas that meets the test requirements.

[0014] The test personnel only need to sample and analyze the flue gas in the pipeline, without on-site sampling. This not only improves the sampling efficiency, but also can simulate the flue gas under different conditions by changing the parameters in the test system, improves the sampling flexibility, and the sampling is less affected by the environment, increasing the accuracy of the subsequent test research.

[0015] Optionally, the flue gas generation system includes at least two pressure tanks for storing different types of gases respectively; the flue gas generation system further includes a mixing tank, which includes a first inlet and a second inlet. The first inlet is communicated with each of the pressure tanks, the second inlet is communicated with a pipeline for supplying clean air, and a first flow control valve is arranged on each pipeline connecting the pressure tank and the mixing tank and on the pipeline for supplying clean air; the outlet of the mixing tank is the outlet of the flue gas generation system.

[0016] Optionally, the outlet of each pressure tank is further communicated with the inlet of the pipeline system, and a second flow control valve is arranged on each connecting pipeline, and a pressure reducing valve is arranged between the second flow control valve and the corresponding pressure tank.

[0017] Optionally, the cavity of the furnace body is of a stepped structure. Along the gas flow direction, the size of the transverse section of the cavity increases successively, and the stepped structure has at least one stepped surface, and one or several stepped surfaces are provided with installation structures for storing denitration catalysts.

[0018] Optionally, it further includes an induced draft fan for providing the gas flow power in the test system; the induced draft fan is arranged downstream of the pipeline system, and the inlet of the induced draft fan is communicated with the outlet of the pipeline system; the pipeline system includes multiple pipe segments, and each pipe segment is provided with the detection component and the air door; the detection component at least includes a temperature sensor, a humidity sensor and a flow sensor. By controlling the working frequencies of each air door and the induced draft fan, the flue gas temperature in each pipe segment is made to be within the corresponding predetermined temperature range, or / and the flue gas humidity in each pipe segment is made to be within the corresponding predetermined humidity range, or / and the flue gas flow rate in each pipe segment is made to be within the corresponding predetermined flow rate range.

[0019] Optionally, the pipeline system includes at least two pipe segments, and the pipe diameter of the latter pipe segment is larger than that of the former pipe segment along the gas flow direction.

[0020] Optionally, the steam generation system includes a steam generator, a regulating valve and a flow meter. The outlet of the steam generator is communicated with each pipe segment through a parallel branch pipeline, and the regulating valve and the flow meter are arranged on each branch pipeline.

[0021] Optionally, each pipe segment of the pipeline system is provided with a through hole, a sampling pipe is installed at the through hole, and a sealing nut is installed at the outer end of the pipe segment of the sampling pipe exposed outside the through hole.

[0022] Optionally, it further includes a control system for controlling the working states of each executing component in the test system and displaying the detection parameters of the detection component on a display component.

[0023] Optionally, the feeding and generating system includes a feeder, a venturi-structured diluter, an air compressor, and a filter; a first branch pipe and a second branch pipe in parallel are connected between the outlet main pipe of the feeder and the inlet of the pipeline system, the diluter is arranged on the second branch pipe, the air compressor is used to provide a gas source for the diluter, and the filter is used to filter excess dust particles discharged from the diluter; the feeding and generating system further includes a control valve for controlling the first branch pipe and the second branch pipe to be in a connected state or a disconnected state.

[0024] In addition, the present invention also provides a method for SO3 sampling and testing using the above test system for simulating different flue gas environments, characterized in that the pipeline system includes a first pipe section, a second pipe section, and a third pipe section connected in sequence, and the diameters of the three increase in sequence, and the inlet of the first pipe section is connected to the gas outlet of the reaction furnace; the SO3 sampling and testing method specifically includes:

[0025] Place a high-vanadium-based catalyst inside the reaction furnace. According to the test simulation requirements, part of the SO2 generated by the flue gas generating system is introduced into the reaction furnace for catalytic oxidation to generate SO3, and the other part is introduced into the outlet pipeline of the reaction furnace;

[0026] According to the test simulation requirements, control the feeding and generating system to inject corresponding amounts of dust into the first pipe section, the second pipe section, and the third pipe section to form corresponding dust concentration conditions in each pipe section;

[0027] Control the flue gas flow rate, temperature, and humidity in the first pipe section, the second pipe section, and the third pipe section, and adjust the internal flue gas temperature range of the first pipe section to be 320°C - 380°C and the humidity range to be 4% - 6% to simulate the flue gas conditions of the actual working condition denitration process, or / and adjust the internal flue gas temperature range of the second pipe section to be 90°C - 150°C and the humidity range to be 4% - 6% to simulate the flue gas conditions in the actual working condition electrostatic precipitator, or / and adjust the internal flue gas temperature range of the third pipe section to be 40°C - 60°C and the humidity to be in a saturated state to simulate the flue gas conditions at the outlet of the actual working condition wet desulfurization or at the inlet and outlet of the wet electrostatic precipitator;

[0028] Among them, the internal flue gas flow rates of the first pipe section, the second pipe section, and the third pipe section increase in sequence, and the concentrations of SO3 in the above three pipe sections decrease in sequence.

[0029] Furthermore, the present invention also provides a method for denitration testing using the above test system for simulating different flue gas environments, characterized in that

[0030] Place the SCR denitration catalyst inside the reaction furnace; according to the test simulation requirements, introduce the standard NO and NH3 gases generated by the flue gas generation system into the reaction furnace, and control the flue gas temperature in the reaction furnace to be between 320°C and 380°C for conventional SCR flue gas denitration simulation, or control the flue gas temperature in the reaction furnace to be between 150 and 320°C for low-temperature SCR flue gas denitration performance simulation to conduct denitration efficiency simulation;

[0031] Or,

[0032] Place the SCR denitration catalyst inside the reaction furnace; according to the test simulation requirements, introduce the standard NO, NH3, and SO2 gases generated by the flue gas generation system into the reaction furnace to test the SO2 / SO3 conversion rate.

[0033] Furthermore, the present invention provides a sampling test method using the above test system for simulating different flue gas environments,

[0034] Under the premise that there is no catalyst in the reaction furnace, introduce the standard NH3, NO, or SO2 gas into the reaction furnace;

[0035] Heat the reaction furnace, and adjust the feed generation system and the steam generation system according to the test requirements to obtain the test flue gas with the required flue gas temperature, humidity, and dust concentration in the pipeline system;

[0036] Measure the NH3 escape concentration, NO x flue gas components or SO2 flue gas components in the test flue gas.

[0037] Finally, the present invention also provides a method for testing the physicochemical properties of the reaction between NH3 and SO3 using the above test system for simulating different flue gas environments,

[0038] Place the high-vanadium catalyst inside the reaction furnace. According to the test simulation requirements, introduce a part of the SO2 generated by the flue gas generation system into the reaction furnace for catalytic oxidation to generate SO3, and at the same time directly introduce a predetermined amount of NH3 standard gas into the outlet flue of the reaction furnace to make the NH3 concentration inside the second pipe section reach a predetermined value;

[0039] Sample and test the SO3 in the outlet pipeline of the reaction furnace to obtain the concentration of SO3 in the flue gas entering the second pipe section; control the flue gas temperature inside the second pipe section, and detect the NH4 + concentration and SO4 2- concentration in the flue gas after the reaction at this temperature; based on the obtained NH4 + concentration and SO4 2- concentration in the flue gas after the reaction, the SO3 sampling test data, and the NH3 introduced into the outlet flue of the reaction furnace, calculate the NH4 + concentration and SO42- The quantitative relationship between;

[0040] By adjusting the flue gas temperature and the NH3 / SO3 molar ratio in the second pipe section, the NH4 concentration and SO4 concentration in the reaction under multiple operating conditions are obtained, + and the quantitative relationship between them is analyzed to study the physical and chemical properties of the reaction between NH3 and SO3. 2- Brief Description of the Drawings The following are structural schematic diagrams of a test system for simulating different flue gas environments in an embodiment of the present invention;

[0041] Figure 1 is a cross-sectional view of the reaction furnace in;

[0042] Figure 2 where Figure 1 the correspondence between the reference numerals and the component names in is:

[0043] Among them, Figures 1 to 2 the correspondence between the reference numerals and the component names in is:

[0044] 1-1 SO2 pressure tank; 1-2 NO pressure tank; 1-3 NH3 pressure tank; 1-41 mass flow control valve; 1-42 second flow control valve; 1-5 pressure reducing valve; 1-6 mass flow control valve; 1-7 air filter; 1-8 mixing tank; 1-9 reaction furnace; 1-91 furnace body; 1-911 stepped surface; 1-91a cavity; 1-92 temperature control device; 1-93 denitration catalyst; 1-94 heat insulation layer;

[0045] 2-1 first pipe section; 2-2 second pipe section; 2-3 third pipe section; 2-5 air filter; 2-6 sampling pipe; 2-7 heat insulation layer; 2-8 induced draft fan; 2-9 hygrometer; 2-10 temperature sensor; 2-11 flow sensor; 2-12 recovery device; 2-41 first air damper, 2-42 second air damper, 2-43 third air damper;

[0046] 3-1 feeder; 3-21 first regulating valve; 3-22 second regulating valve; 3-23 third regulating valve; 3-3 diluter; 3-4 air compressor; 3-5 filter;

[0047] 4-1 steam generator; 4-2 regulating valve; 4-3 flowmeter;

[0048] 5- control system. Detailed Embodiments

[0049] In view of the technical problems existing in the prior art, in-depth research has been carried out in this article, and a test system is proposed that can accurately obtain flue gas under different environmental conditions and is conducive to shortening the subsequent research and test cycle.

[0050] To enable those skilled in the art to better understand the technical solution of the present invention, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0051] Please refer to Figure 1 and Figure 2 , Figure 1 which is a schematic structural diagram of a test system for simulating different flue gas environments in an embodiment of the present invention; Figure 2 is Figure 1 a cross-sectional view of the reaction furnace in

[0052] The present invention provides a test system for simulating different flue gas environments, including a flue gas generation system, a feeding and generating system, a steam generation system, a reaction furnace 1-9, and a pipeline system.

[0053] Among them, the flue gas generation system is mainly used to generate the gas components in the test flue gas. Of course, according to the test requirements, the flue gas generation system can generate the main gas components in the test flue gas. Usually, flue gas contains gas components such as NO x , SO2, SO3, NH3, etc., all of which can be generated by the flue gas generation system 1. And the main component of NO x gas in the flue gas is NO. In order to reduce the test cost of the test system and simplify the system structure, in this paper, it is preferably to use NO standard gas to replace NO x in the test flue gas.

[0054] In addition to the gas components in the flue gas, there are also solid dust particles. In order to accurately simulate the flue gas in different environments, the feeding and generating system in the present invention is used to generate the solid dust particles in the test flue gas.

[0055] The steam generation system is used to generate the steam in the test flue gas. Specifically, the steam generation system 4 only needs to be able to form steam, and its specific structure can refer to the existing technology.

[0056] The reaction furnace 1-9 in the present invention includes a furnace body 1-91 forming a cavity. The furnace body 1-91 is provided with a gas inlet and a gas outlet communicating with the cavity. The gas inlet is used to communicate with the outlet of the flue gas generation system 1; an installation structure for storing the denitration catalyst 1-93 is also provided in the cavity, which mainly considers eliminating the nitrogen element in the gas. The denitration catalyst is a mature material in the existing technology, and its installation is also relatively mature. Therefore, the specific structure of the installation structure in the cavity is not disclosed in this paper, which will not prevent those skilled in the art from understanding and implementing the technical solution.

[0057] The reactor 1-9 further includes a temperature control device 1-92 for heating the cavity, which is used to heat the cavity of the reactor 1-9. In this way, the temperature of the cavity 1-91a can be adjusted to the actual temperature of the denitration reaction, and the temperature of the cavity 1-91a can also be adjusted to the heating temperature required to simulate the actual desulfurization and wet electrostatic environment in the subsequent pipeline system.

[0058] The actual temperature of the denitration reaction usually requires the flue gas temperature to be 320-380°C or 150-320°C to meet the experimental temperature requirements such as conventional SCR flue gas denitration or low-temperature SCR flue gas denitration.

[0059] The temperature of desulfurization and wet electrostatic is relatively low, generally below 80°C. However, to avoid the adsorption loss of the generated flue gas in the reactor, the temperature in the reactor is required to be higher than 300°C, and then the temperature is reduced by adjusting the flow rate of the pipeline system.

[0060] Therefore, the temperature control device 1-92 in the present invention can adjust the temperature in the reactor 1-9 to the corresponding above temperatures to meet the required temperatures of different tests.

[0061] The temperature control device 1-92 includes a heating device and a temperature control component, and the specific structure will not be described in detail herein.

[0062] The pipeline system in the present invention is arranged downstream of the reactor 1-9, and its inlet is connected to the gas outlet of the reactor 1-9, that is, the gas enters the pipeline system after passing through the reactor 1-9.

[0063] Moreover, the outlets of the feeding generation system and the steam generation system are both connected to the pipeline system, and a detection component is arranged on the pipe wall of the pipeline system for detecting the flue gas parameters in the pipeline. The flue gas parameters can include parameters such as flue gas temperature, humidity, flow rate, and dust concentration. The detection component includes one or several of the following: a hygrometer, a thermometer, and a differential pressure flowmeter to detect the humidity, temperature, and flow rate of the flue gas. In this way, the operator can adjust the parameters of other test systems through the detection parameters of the detection component to make the various parameters of the flue gas in the pipeline meet the preset requirements.

[0064] From the above description, it can be seen that the test system provided by the present invention can generate the main components such as gas components, solid dust particles, and steam in the test flue gas. The temperature control device can heat the cavity of the reactor 1-9, which can provide the actual temperature of the denitration reaction and the heating temperature actually required to simulate desulfurization and wet electrostatic in the subsequent pipeline system. The reacted gas is introduced into the pipeline system, and the flue gas parameters in the pipeline can be detected by the detection component arranged on the pipeline system, and then the flow rates of the gas components, solid dust particles, and steam are adjusted to obtain the simulated flue gas that meets the test requirements.

[0065] The test personnel only need to sample and analyze the flue gas in the pipeline without on-site sampling, which not only improves the sampling efficiency, but also can simulate the flue gas under different conditions by changing the parameters in the test system, improving the sampling flexibility, with little environmental impact on sampling and increasing the accuracy of later experimental research.

[0066] The test system provided in this paper can meet the simulation of flue gas such as SO3 sampling test of flue gas, experimental research on denitrification performance, NH3 escape sampling test, flue gas composition test, and physicochemical property test of the reaction between NH3 and SO3 (the influence of NH3 / SO3 molar ratio on the formation of ammonium bisulfate (ABS)).

[0067] In a specific embodiment, the flue gas generation system may include at least two pressure tanks, which are respectively used to store different types of gases; a schematic diagram of setting three pressure tanks is given in the figure. The three pressure tanks are respectively used to contain SO2 gas, NO gas and NH3 gas, which are defined as SO2 pressure tank 1-1, NO pressure tank 1-2 and NH3 pressure tank 1-3 in this paper. Of course, the number of pressure tanks set is not limited to the description in this paper and can also be other numbers.

[0068] The flue gas generation system may also include a mixing tank 1-8. The mixing tank 1-8 includes a first inlet and a second inlet. The first inlet is connected to each pressure tank, and the second inlet is connected to the pipeline supplying clean air. An air filter 1-7 may also be provided on the clean air pipeline. The power for the clean air to enter the mixing tank can be provided by the induced draft fan set in the system. Of course, a power device can also be set separately to provide the flowing power for the clean air.

[0069] And a first flow control valve is provided on the connecting pipe between each pressure tank and the mixing tank 1-8 and on the pipeline supplying clean air; the first flow control valve can be a mass flow control valve. As shown in the figure, a mass flow control valve 1-6 is provided on the clean air pipeline, and the flow rate of the clean air is controlled by the mass flow control valve 1-6; a mass flow control valve 1-41 is provided on the outlet pipeline of each pressure tank, and each pressure tank supplies gas to the inside of the mixing tank through the corresponding mass flow control valve. The opening degrees of the mass flow control valves can be controlled by the control system, and by changing the opening degrees of the mass flow control valves, clean air with different flow rates can enter the mixing tank to be mixed with the standard gas flowing out of the pressure tank. Each pressure tank can correspond to the mass flow control valve 1-41 one by one, or can be controlled by a mass flow control valve assembly. The mass flow controllers respectively measure the mass flow rates of the standard gases as

[0070] In addition, in order to supply gas to the outside stably from the pressure tank, a pressure reducing valve 1-5 can also be installed upstream of the mass flow control valve.

[0071] As described above, the outlet of the mixing tank 1-8 is the gas outlet of the flue gas generation system. That is to say, before each gas component and clean air enter the reaction furnace 1-9, they are first mixed evenly inside the mixing tank 1-8 and then introduced into the reaction furnace 1-9 for heating or denitrification reaction.

[0072] The flue gas generation system with the above structure has a relatively simple structure and is relatively convenient to control.

[0073] In order to accurately simulate the composition of the flue gas, the following settings are also made in this article.

[0074] The outlets of the pressure tanks in the present invention are further connected to the inlets of the pipeline system. That is to say, the outlets of the pressure tanks in this article are provided with a first pipeline and a second pipeline in parallel. The outlet of the pressure tank is connected to the first inlet of the mixing tank through the first pipeline, and at the same time, the outlet of the pressure tank can also be connected to the inlet of the pipeline system through the second pipeline.

[0075] In this way, the gas in each pressure tank can directly enter the pipeline system downstream of the reaction furnace 1-9 to increase the corresponding gas components. And in order to accurately control the amount of added gas, a second flow control valve 1-42 is further provided on the connecting pipeline between each pressure tank and the inlet of the pipeline system. The structure of the second flow control valve can refer to the structure of the first flow control valve. Of course, a pressure reducing valve 1-5 can also be provided between the second flow control valve and the outlet of the pressure tank to stabilize the flow rate. Taking the second flow control valve as a mass flow control valve as an example, the mass flow rates of the standard gases measured by the gas mass flow control valve 1-42 of this path are QSO2,o, QNO,o, and QNH3,o respectively.

[0076] In order to facilitate the installation of the denitrification catalyst layer, the cavity of the furnace body 1-91 can be a stepped structure. Along the gas flow direction, the size of the cross section of the cavity 1-91a increases in sequence, and the stepped structure has at least one stepped surface 1-911, and one or several stepped surfaces 1-911 are provided with installation structures for storing the denitrification catalyst 1-93. The distance between adjacent stepped surfaces needs to meet the installation of the catalyst layer. The catalyst layer can be installed in one layer, or two layers or more layers.

[0077] In order to maintain the test temperature required for the cavity of the reaction furnace 1-9, a heat preservation layer 1-94 can also be provided on the periphery of the furnace body 1-91.

[0078] The test system in the above embodiments can also include an induced draft fan 2-8 for providing the gas flow power in the test system; the induced draft fan 2-8 is arranged downstream of the pipeline system, and the inlet of the induced draft fan 2-8 is connected to the outlet of the pipeline system. Under the action of the induced draft fan 2-8, clean air enters the mixing tank 1-8, and the gas in the mixing tank 1-8 can flow into the subsequent pipeline system.

[0079] The pipeline system includes multiple pipe segments, and a detection component and a damper are provided on each pipe segment; the detection component at least includes a hygrometer 2-9, a temperature sensor 2-10, and a flow sensor 2-11. By controlling the working frequencies of each damper and the induced draft fan, the flue gas temperature in each pipe segment is made to be within a corresponding predetermined temperature range, and / or the flue gas humidity in each pipe segment is made to be within a corresponding predetermined humidity range, and / or the flue gas flow rate in each pipe segment is made to be within a corresponding predetermined flow rate range.

[0080] That is to say, by adjusting the opening degree of the damper on each pipe segment, the corresponding pipe segment can be adjusted to the required test temperature and the gas flow rate in the pipe can be adjusted to the predetermined flow rate range required by the test. In this way, flue gas at different flow rates and temperatures can be obtained, greatly improving the diversity of the system's simulated flue gas.

[0081] An air filter 2-5 can also be provided on the connecting pipeline of each damper, and a recovery device 2-12 is also provided at the outlet of the induced draft fan 2-8.

[0082] Specifically, the pipeline system includes at least two pipe segments. Along the gas flow direction, the diameter of the latter pipe segment is larger than that of the former pipe segment. The adjacent pipe segments can be detachably connected. The embodiment in which the pipeline system includes three pipe segments is shown in the figure, which are respectively defined as the first pipe segment 2-1, the second pipe segment 2-2, and the third pipe segment 2-3. Among them, the diameters of the first pipe segment 2-1, the second pipe segment 2-2, and the third pipe segment 2-3 increase in sequence, and the adjacent pipe segments are connected by a tapered pipe for transition. The diameters of the first pipe segment 2-1, the second pipe segment 2-2, and the third pipe segment 2-3 are D1, D2, and D3 respectively, and D1 < D2 < D3. During the experiment, the number of pipeline connections can also be increased or decreased according to the experimental needs, and the pipeline length can be changed, etc.

[0083] Correspondingly, a first damper 2-41, a second damper 2-42, and a third damper 2-43 are respectively provided corresponding to the first pipe segment 2-1, the second pipe segment 2-2, and the third pipe segment 2-3.

[0084] In order to facilitate the sampling of the flue gas in the pipeline system, each pipe segment is provided with a through hole, and a sampling pipe 2-6 is installed at the through hole. A sealing nut is installed at the outer end of the pipe segment where the sampling pipe 2-6 extends outside the through hole. The operator samples the flue gas inside the pipeline through the sampling pipe 2-6. When not sampling, the outer end of the sampling pipe is sealed by the sealing nut.

[0085] In order to keep the temperature inside each pipe segment of the pipeline system constant, a heat insulation layer 2-7 can also be provided on the outside of each pipe segment.

[0086] In the above embodiments, the vapor generation system may include a vapor generator 4-1, a regulating valve 4-2, and a flow meter 4-3. The outlet of the vapor generator is respectively connected to each pipe section through a parallel branch pipeline, and a regulating valve 4-2 and a flow meter 4-3 are provided on each branch pipeline. For the embodiment in which the above pipeline system includes a first pipe section 2-1, a second pipe section 2-2, and a third pipe section 2-3, the outlet pipeline of the vapor generator 4-1 also includes a first branch pipeline, a second branch pipeline, and a third branch pipeline, on which a regulating valve 4-2 and a flow meter 4-3 are provided.

[0087] In order to achieve automatic control, the test system in the above embodiments may further include a control system 55 for controlling the working states of the various actuating components in the test system and displaying the detection parameters of the detection components on the display component.

[0088] The control system may internally store information such as the temperature, flow rate, dust content, and gas components of the flue gas to be obtained in the test. By controlling the working states of various components such as the regulating valves, flow valves, and working power of the induced draft fan in the control system 5, the flue gas required for the test can be finally obtained.

[0089] In the above embodiments, the feeding and generating system may include a feeder 3-1, a venturi-structured diluter 3-3, an air compressor 3-4, and a filter 3-5. A parallel first branch pipe and a second branch pipe are connected between the outlet main pipe of the feeder 3-1 and the inlet of the pipeline system. A diluter 3-3 is provided on the second branch pipe. The air compressor 3-4 is used to provide a gas source for the diluter 3-3, and the filter is used to filter the excess dust particles discharged from the diluter.

[0090] The feeding and generating system further includes a control valve for controlling the first branch pipe and the second branch pipe to be in a connected state or a disconnected state. When the control valve is in the first working state, the first branch pipe is in a connected state and the second branch pipe is in a disconnected state; when the control valve is in the second working state, the first branch pipe is in a disconnected state and the second branch pipe is in a connected state.

[0091] When the first branch pipe is connected and the second branch pipe is disconnected, the outlet main pipe of the feeder is directly connected to the inlet pipe of the pipeline system, so that the solid particles in the feeder can directly enter the pipeline system to meet the simulation of flue gas with a large dust content. When the second branch pipe is connected and the first branch pipe is disconnected, the material flowing out of the feeder outlet enters the inlet of the pipeline system after passing through the diluter under the action of the air compressor and the venturi-effect diluter, so that the simulation of flue gas with a relatively small dust content can be satisfied.

[0092] The control valve can be a single component or two or more relatively independent valves. This text provides an implementation of a control valve including three regulating valves. The control valve includes a first regulating valve 3-21, a second regulating valve 3-22, and a third regulating valve 3-23. The first regulating valve 3-21 is arranged on the first branch pipe, and the second regulating valve 3-22 and the third regulating valve 3-23 are arranged on the second branch pipe.

[0093] When the experiment requires providing low-concentration dust, to ensure that the feeding system can continuously and uniformly feed a small amount of material, the feeding amount of the feeder 3-1 can be appropriately increased through the auxiliary action of the diluter 3-3 designed according to the Venturi structure principle and a certain cross-sectional area ratio to improve the feeding stability. During the experiment, the first regulating valve 3-21 can be closed, and the second regulating valve 3-22 and the third regulating valve 3-23 can be opened to ensure that the dust discharged from the feeder 3-1 first passes through the diluter 3-3 for dilution and then enters the pipeline system 2. The diluter 3-3 is supplied with air by an air compressor 3-4. After the dust entering the diluter 3-3 is diluted, the excess dust to be discharged is filtered by a filter 3-5 to avoid direct discharge into the air.

[0094] Of course, the feeder 3-1 can control the feeding frequency through a frequency conversion controller to achieve different rotation speeds and provide different feeding powers. At the same time, different feeding amounts can also be achieved by connecting different feeding screws (such as different pitches and depths of the threads of the feeding screws). Through the above different combinations, the feeding amount requirements for different inlet dust concentrations can be met.

[0095] The structure and specific installation method of the diluter 3-3 with a Venturi structure are not specifically described in this text, which does not prevent those skilled in the art from understanding and implementing this technical solution.

[0096] Through the above test system, research on the sampling and testing method of flue gas SO3, research on denitrification performance experiments, research on the sampling and testing method of NH3 escape, research on the testing method of flue gas components, research on the physical and chemical properties of the reaction between NH3 and SO3, etc. can be achieved.

[0097] The following specifically introduces several specific methods for performing simulation tests using the above test system.

[0098] I. SO3 Sampling and Testing Method

[0099] Specifically, the pipeline system in the above test system includes a first pipe section 2-1, a second pipe section 2-2, and a third pipe section 2-3 connected in sequence, with their diameters increasing in sequence. The inlet of the first pipe section 2-1 is connected to the gas outlet of the reaction furnace 1-9. The SO3 sampling and testing method specifically includes:

[0100] Placing a high-vanadium catalyst inside the reaction furnace 1-9;

[0101] According to the test simulation requirements, part of the SO2 generated by the flue gas generation system is introduced into the reactor 1-9, and the other part is introduced into the outlet pipe of the reactor 1-9; in this test method, only SO2 is introduced into the reactor 1-9, and the reactor 1-9 is only used as a standard generator of flue gas SO3.

[0102] According to the test simulation requirements, the flue gas in the first pipe section 2-1, the second pipe section 2-2, and the third pipe section 2-3 is controlled to achieve the dust concentration, flue gas flow rate, temperature, and humidity required for the test. Specifically, the feed generation system is controlled to inject a corresponding amount of dust into the first pipe section 2-1, the second pipe section 2-2, and the third pipe section 2-3 to form corresponding dust concentration conditions in each pipe section. The fan and damper openings are adjusted to form the flue gas flow rate and flue gas temperature required by the predetermined experiment in each pipe section. The steam generation system is controlled to adjust the flue gas humidity in each pipe section. The predetermined experimental parameters required in each pipe section may be different.

[0103] Through the above-mentioned parameter control, the internal flue gas temperature range of the first pipe section 2-1 is adjusted to 320°C-380°C and the humidity range is 4%-6% to simulate the flue gas conditions of the denitrification process in actual working conditions, or / and the internal flue gas temperature range of the second pipe section 2-2 is adjusted to 90°C-150°C and the humidity range is 4%-6% to simulate the electrostatic precipitator flue gas conditions in actual working conditions, or / and the internal flue gas temperature range of the third pipe section 2-3 is adjusted to 40°C-60°C and the humidity is saturated to simulate the flue gas conditions at the wet desulfurization outlet or the wet electrostatic precipitator inlet and outlet in actual working conditions.

[0104] Among them, the flue gas flow rates inside the first pipe section 2-1, the second pipe section 2-2 and the third pipe section 2-3 increase in sequence, and the concentrations of SO3 in the above three pipe sections decrease in sequence.

[0105] Through the above simulation methods, different flue gas temperatures, humidity, dust concentrations, and different flue gas SO2, SO3 concentrations and other working flue gas conditions can be simulated respectively, as well as the flue gas SO3 sampling test method under different working flue gas conditions can be studied.

[0106] The flue gas SO3 required in the pipeline system is mainly generated by catalytic oxidation of SO2 under the action of high temperature and high vanadium catalyst in the reactor. After entering the pipeline system, due to the lack of catalyst in the first pipe section 2-1, the second pipe section 2-2 and the third pipe section 2-3, the mass flow rate of the flue gas SO3 inside the pipeline system remains unchanged according to the law of conservation of mass. Therefore, by collecting flue gas SO3 in the first pipe section 2-1, the second pipe section 2-2 and the third pipe section 2-3 and calculating the mass flow rate of flue gas SO3, it can be used to evaluate the accuracy of the flue gas SO3 sampling and testing method under different operating conditions.

[0107] 2. Denitrification test method

[0108] Place the SCR denitration catalyst inside the reaction furnace 1-9; according to the test simulation requirements, introduce the standard NO and NH3 gases generated by the flue gas generation system into the reaction furnace 1-9, and control the flue gas temperature in the reaction furnace 1-9 to be between 320°C and 380°C for conventional SCR flue gas denitration simulation, or control the flue gas temperature in the reaction furnace 1-9 to be between 150 and 320°C for low-temperature SCR flue gas denitration performance simulation to meet the needs of full-load denitration technology research and low-temperature catalyst research.

[0109] Specifically, the key technical indicators related to the denitration performance can also be calculated through the following simplified calculation formula:

[0110] 2.1 Ammonia-nitrogen molar ratio (NH3 / NO x )

[0111]

[0112] In the formula: n—the ammonia-nitrogen molar ratio (NH3 / NO x )

[0113] —The mass flow rate of the NH3 standard gas at the inlet of the reaction furnace 1-9, unit: L / min;

[0114] —The concentration of the NH3 standard gas, unit: ppm;

[0115] Q NO,i —The mass flow rate of the NO standard gas at the inlet of the reaction furnace 1-9, unit: L / min;

[0116] C NO,b —The concentration of the NO standard gas, unit: ppm.

[0117] 2.2 Theoretical flue gas composition at the inlet of the reaction furnace 1-9

[0118] Through the standard gas concentration, the standard gas mass flow rate, and the flow rate monitored at the outlet of the reaction furnace 1-9, the concentration of the theoretical flue gas composition entering the reaction furnace 1-9 can be calculated:

[0119]

[0120] In the formula: C i —The concentration of the theoretical flue gas composition at the inlet of the reaction furnace 1-9, unit: mg / Nm 3 ;

[0121] M—the molar mass of the standard gas, unit: g;

[0122] 22.4—the molar volume of the standard gas, unit: L;

[0123] C b —— Standard gas concentration, unit: ppm;

[0124] Q1—— Standard gas mass flow rate, unit: L / min;

[0125] Q o —— Flue gas flow rate at the outlet of reactors 1-9, unit: Nm 3 / h.

[0126] 2.3 Denitrification efficiency

[0127] Use a flue gas analyzer to measure the NO concentration of the flue gas at the outlets of reactors 1-9, and calculate the NO x concentration and denitrification efficiency.

[0128]

[0129] Where: —— Denitrification efficiency, %;

[0130] —— NO at the inlets of reactors 1-9 x concentration, mg / Nm 3 ;

[0131] —— NO at the outlets of reactors 1-9 x concentration, mg / Nm 3 .

[0132] The above parameters can be measured by detection components installed at corresponding positions.

[0133] 2.4 SO2 / SO3 conversion rate

[0134] In another test method, place the SCR denitrification catalyst inside reactors 1-9; according to the test simulation requirements, introduce the standard gases of NO, NH3, and SO2 generated by the flue gas generation system into reactors 1-9. By measuring the introduced amount of SO2 and sampling and testing the flue gas SO3 at the outlets of reactors 1-9 using the control condensation method or the isopropanol absorption method, the flue gas SO3 concentration and SO2 / SO3 conversion rate can be calculated.

[0135]

[0136] Where: x—— SO2 / SO3 conversion rate, %;

[0137] —— Molar mass of SO2, g / mol;

[0138] —— Molar mass of SO3, g / mol;

[0139] —— Measured SO3 concentration at the outlets of Reactors 1 - 9, mg / Nm 3 ;

[0140] —— Theoretical SO2 concentration at the inlets of Reactors 1 - 9, mg / Nm 3 。

[0141] III. NH3 Slip Concentration Test and Flue Gas Composition Sampling Test Methods

[0142] Under the premise that there is no catalyst in Reactors 1 - 9, introduce NH3, NO or SO2 standard gas into Reactors 1 - 9; at this time, Reactors 1 - 9 only serve as heating devices;

[0143] Heat Reactors 1 - 9, and adjust the feed generation system and steam generation system according to the test requirements to obtain test flue gas with the required flue gas temperature, humidity and dust concentration in the pipeline system;

[0144] Measure the NH3 slip concentration, NO x flue gas composition or SO2 flue gas composition in the test flue gas.

[0145] In the above test method, when only NH3 is introduced, the NH3 slip concentration test research can be realized. For example, test methods such as chemical absorption method and laser method for NH3 slip can be studied at the pipeline system location. By comparing the measured NH3 slip concentration with the theoretical NH3 slip concentration at the inlets of Reactors 1 - 9, it can be used to verify the accuracy of the NH3 slip test.

[0146] When only NO or SO2 standard gas is introduced into Reactors 1 - 9, and the feed generation system is adjusted to achieve different feed amounts and the steam generation system is adjusted to achieve different steam supply amounts, different working conditions of flue gas temperature, humidity and dust concentration can be formed in the first pipe section 2 - 1, the second pipe section 2 - 2 and the third pipe section 2 - 3. NO can be carried out at the monitoring holes of the first pipe section 2 - 1, the second pipe section 2 - 2 and the third pipe section 2 - 3 x and SO2 flue gas composition test research. By comparing the measured flue gas composition concentration with the theoretical flue gas composition concentration at the inlets of Reactors 1 - 9, it can be used to verify the accuracy of the flue gas composition test.

[0147] IV. Physicochemical Property Test Method for the Reaction of NH3 and SO3

[0148] In the air preheater, the flue gas temperature is reduced. Since SO3 in the flue gas is extremely easy to combine with water vapor to form SO3 / H2SO4, and there is a certain amount of escaped NH3 in SCR denitration, the generated H2SO4 can react with the escaped NH3 to form ammonium sulfate or ammonium bisulfate (ABS). In the temperature section of the air preheater, ammonium bisulfate is in the stage of changing from liquid to solid, with extremely strong adsorbability, and it is very easy to adsorb on the dust, increasing the viscosity of the dust, thus causing the blockage of the air preheater.

[0149] Therefore, by placing a high-vanadium catalyst inside the reaction furnace (1-9), a part of the SO2 generated by the flue gas generation system is introduced into the reaction furnace (1-9) according to the test simulation requirements to catalytically oxidize and generate SO3, and at the same time, a predetermined amount of NH3 standard gas is directly introduced into the outlet flue of the reaction furnace 1-9 so that the NH3 concentration inside the second pipe section 2-2 reaches a predetermined value; the pipeline system can refer to the above description and will not be elaborated here.

[0150] Sample and test SO3 in the outlet pipeline of the reaction furnace 1-9 to obtain the concentration of SO3 in the flue gas entering the second pipe section 2-2; control the flue gas temperature inside the second pipe section 2-2 and detect the NH4 + concentration and SO4 2- concentration in the flue gas after reaction at this temperature; based on the obtained NH4 + concentration and SO4 2- concentration, the SO3 sampling test data, and the NH3 introduced into the outlet flue of the reaction furnace 1-9, calculate the quantitative relationship between the NH4 + concentration and SO4 2- after reaction;

[0151] By adjusting the flue gas temperature and the NH3 / SO3 molar ratio inside the second pipe section 2-2, obtain the quantitative relationship between the NH4 + concentration and SO4 2- after reaction under multiple working conditions, and analyze the physical and chemical properties of the reaction between NH3 and SO3.

[0152] The research on the physical and chemical properties of the reaction between NH3 and SO3 aims to provide the environmental conditions required for simulating the reaction between NH3 and SO3. At the same time, through research, it can be used to analyze the problem of air preheater blockage caused by the reaction between escaped NH3 and SO3 in the air preheater. The research on the test analysis method after the reaction between NH3 and SO3 has been studied by relevant field personnel and will not be the focus of this embodiment, so it will not be elaborated in this embodiment.

[0153] The main reactions between NH3 and SO3 in the simulated flue are as follows:

[0154] NH3 + SO3 + H2O = NH4HSO4 (i.e., ABS) and 2NH3 + SO3 + H2O = (NH4)2SO4

[0155] The above has introduced in detail a test system and a test method for simulating different flue gas environments provided by the invention. Specific examples are used in this article to elaborate on the principle and implementation manner of the invention. The description of the above embodiments is only used to help understand the method and its core idea of the invention. It should be noted that for those of ordinary skill in the art of this technology, without departing from the principle of the invention, several improvements and modifications can still be made to the invention, and these improvements and modifications also fall within the protection scope of the claims of the invention.

Claims

1. A test system for simulating different flue gas environments, characterized in that It includes the following components: A flue gas generation system for generating the gas components in the test flue gas; A feeding and generation system for generating the solid dust particles in the test flue gas; A steam generation system for generating the steam in the test flue gas; A reaction furnace (1-9), including a furnace body (1-91) forming a cavity (1-91a), the furnace body (1-91) being provided with a gas inlet and a gas outlet communicating with the cavity, the gas inlet being used for communicating with the outlet of the flue gas generation system; an installation structure for storing a catalyst is also provided in the cavity; the reaction furnace (1-9) further includes a temperature control device for heating the cavity (1-91a); A pipeline system is arranged downstream of the reaction furnace (1-9), its inlet communicates with the gas outlet of the reaction furnace, the outlets of the feeding and generation system and the steam generation system can both communicate with the pipeline system, and a detection component is arranged on the pipe wall of the pipeline system for detecting the flue gas parameters in the pipeline; It further includes an induced draft fan (2-8) for providing the gas flow power in the test system; the induced draft fan (2-8) is arranged downstream of the pipeline system, and the inlet of the induced draft fan (2-8) communicates with the outlet of the pipeline system; the pipeline system includes multiple pipe segments, and each pipe segment is provided with the detection component and a damper; the detection component at least includes a temperature sensor, a humidity sensor and a flow sensor, and by controlling the working frequencies of each damper and the induced draft fan (2-8), the flue gas temperature in each pipe segment is made to be within a corresponding predetermined temperature range, or / and the flue gas humidity in each pipe segment is made to be within a corresponding predetermined humidity range, or / and the flue gas flow rate in each pipe segment is made to be within a corresponding predetermined flow rate range.

2. The test system for simulating different flue gas environments according to claim 1, wherein The flue gas generation system includes at least two pressure tanks respectively for storing different types of gases; the flue gas generation system further includes a mixing tank (1-8), the mixing tank (1-8) includes a first inlet and a second inlet, the first inlet communicates with each of the pressure tanks, the second inlet communicates with a pipeline for supplying clean air, and a first flow control valve is arranged on each pipeline connecting each pressure tank and the mixing tank (1-8) and on the pipeline for supplying clean air; the outlet of the mixing tank is the outlet of the flue gas generation system; Or / and, the outlets of each of the pressure tanks further communicate with the inlet of the pipeline system, and a second flow control valve is arranged on each connecting pipeline, and a pressure reducing valve is also arranged between the second flow control valve and the corresponding pressure tank.

3. The test system for simulating different flue gas environments according to claim 1, characterized in that The cavity of the furnace body (1-91) is of a stepped structure, and along the gas flow direction, the size of the transverse section of the cavity increases in sequence, and the stepped structure has at least one stepped surface, and one or several stepped surfaces are provided with an installation structure for storing a denitration catalyst.

4. The test system for simulating different flue gas environments according to claim 1, wherein The pipeline system includes at least two pipe segments. Along the gas flow direction, the diameter of the latter pipe segment is larger than that of the previous adjacent pipe segment. The steam generation system includes a steam generator (4-1), a regulating valve, and a flowmeter. The outlet of the steam generator is connected to each pipe segment through parallel branch pipelines, and the regulating valve and the flowmeter are provided on each of the branch pipelines.

5. The test system for simulating different flue gas environments according to claim 1, wherein Each pipe segment of the pipeline system is provided with a through hole, and a sampling pipe (2-6) is installed at the through hole. A sealing nut is installed at the outer end of the pipe segment where the sampling pipe (2-6) extends outside the through hole.

6. The test system for simulating different flue gas environments according to claim 1, characterized in that, It further includes a control system for controlling the working states of the various actuating components in the test system and displaying the detection parameters of the detection components on a display component.

7. The test system for simulating different flue gas environments according to any one of claims 1 to 6, characterized in that, The feeding and generating system includes a feeder (3-1), a venturi-structured diluter (3-3), an air compressor (3-4), and a filter (3-5). A first branch pipe and a second branch pipe in parallel are connected between the outlet main pipeline of the feeder (3-1) and the inlet of the pipeline system. The diluter (3-3) is provided on the second branch pipe. The air compressor (3-4) is used to provide a gas source for the diluter (3-3), and the filter (3-5) is used to filter the excess dust particles discharged from the diluter (3-3). The feeding and generating system further includes a control valve for controlling the first branch pipe and the second branch pipe to be in a connected state or a disconnected state.

8. A method for SO3 sampling and testing using the test system for simulating different flue gas environments according to any one of claims 1 to 7, characterized in that, The pipeline system includes a first pipe segment (2-1), a second pipe segment (2-2), and a third pipe segment (2-3) connected in sequence, and their diameters increase in sequence. The inlet of the first pipe segment (2-1) is connected to the gas outlet of the reaction furnace (1-9). The specific SO3 sampling and testing method includes: Place a high-vanadium-based catalyst inside the reaction furnace (1-9). According to the test simulation requirements, part of the SO2 generated by the flue gas generation system is introduced into the reaction furnace (1-9) for catalytic oxidation to generate SO3, and the other part is introduced into the outlet pipeline of the reaction furnace (1-9). According to the test simulation requirements, control the feeding and generating system to inject corresponding amounts of dust into the first pipe segment (2-1), the second pipe segment (2-2), and the third pipe segment (2-3) to form corresponding dust concentration conditions in each pipe segment. Adjust the opening degrees of the induced draft fan and the dampers on the corresponding pipe segments to form the flue gas flow rate and flue gas temperature required by the predetermined experiment in each pipe segment, and control the steam generation system to adjust the flue gas humidity in each pipe segment. Among them, the flue gas temperature range inside the first pipe segment (2-1) is 320°C - 380°C, and the humidity range is 4% - 6% to simulate the flue gas conditions of the denitration process under actual working conditions. Or / and adjust the flue gas temperature range inside the second pipe segment (2-2) to be 90°C - 150°C, and the humidity range is 4% - 6% to simulate the flue gas conditions in the electrostatic precipitator under actual working conditions. Or / and adjust the flue gas temperature range inside the third pipe segment (2-3) to be 40°C - 60°C, and the humidity is in a saturated state to simulate the flue gas conditions at the outlet of the wet flue gas desulfurization or at the inlet and outlet of the wet electrostatic precipitator under actual working conditions. Moreover, the flue gas flow rates inside the first pipe section (2-1), the second pipe section (2-2), and the third pipe section (2-3) increase in sequence, while the concentrations of SO3 in the above three pipe sections decrease in sequence.

9. A denitration test method using the test system for simulating different flue gas environments according to any one of claims 1 to 7, characterized in that a catalyst for SCR denitration is placed inside the reaction furnace (1-9); NO and NH3 standard gases generated by the flue gas generation system are introduced into the reaction furnace (1-9) according to the test simulation requirements, and the flue gas temperature in the reaction furnace (1-9) is controlled to be between 320°C and 380°C for conventional SCR flue gas denitration simulation, or the flue gas temperature in the reaction furnace (1-9) is controlled to be between 150°C and 320°C for low-temperature SCR flue gas denitration performance simulation, so as to perform denitration efficiency simulation; Or, a catalyst for SCR denitration is placed inside the reaction furnace (1-9); NO, NH3, and SO2 standard gases generated by the flue gas generation system are introduced into the reaction furnace (1-9) according to the test simulation requirements, and the SO2 / SO3 conversion rate is measured.

10. A sampling test method using the test system for simulating different flue gas environments according to any one of claims 1 to 7, characterized in that NH3, NO, or SO2 standard gas is introduced into the reaction furnace (1-9) on the premise that there is no catalyst in the reaction furnace (1-9); the reaction furnace (1-9) is heated, and the feeding and gas generation systems are adjusted according to the test requirements to obtain test flue gas with the required flue gas temperature, humidity, and dust concentration in the pipeline system; Measure the NH3 escape concentration and NO in the test flue gas x flue gas components or SO2 flue gas components.

11. A method for testing the physicochemical properties of the reaction between NH3 and SO3 using the test system for simulating different flue gas environments according to any one of claims 1 to 7, characterized in that the pipeline system includes a first pipe section (2-1), a second pipe section (2-2), and a third pipe section (2-3) connected in sequence, the diameters of the three increase in sequence, and the inlet of the first pipe section (2-1) is connected to the gas outlet of the reaction furnace (1-9); a high-vanadium catalyst is placed inside the reaction furnace (1-9), and a part of the SO2 generated by the flue gas generation system is introduced into the reaction furnace (1-9) according to the test simulation requirements to be catalytically oxidized to generate SO3, and a predetermined amount of NH3 standard gas is directly introduced into the outlet flue of the reaction furnace (1-9) so that the NH3 concentration inside the second pipe section (2-2) reaches a predetermined value; Sample and test SO3 in the outlet pipeline of the reactor (1-9) to obtain the concentration of SO3 in the flue gas entering the interior of the second pipe section (2-2); control the temperature of the flue gas in the second pipe section (2-2), and detect the NH4 + concentration and SO4 2- concentration in the flue gas after the reaction at this temperature; based on the obtained NH4 + concentration and SO4 2- concentration, the SO3 sampling and test data, and the NH3 introduced into the outlet flue of the reactor (1-9), calculate the quantitative relationship between the NH4 + concentration and SO4 2- concentrations; By adjusting the flue gas temperature and NH3 / SO3 molar ratio in the second pipe section (2-2), the NH4 + concentration and SO4 2- quantity relationship under multiple operating conditions obtained, and the physical and chemical properties of the reaction between NH3 and SO3 are analyzed.

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