Method and system for evaluating performance of a continuous catalytic cracking flue gas desulfurization and denitrification aid

Abstract

The present disclosure relates to a continuous catalytic cracking flue gas desulfurization and denitrification additive performance evaluation method and system, comprising the following steps: making the raw main agent pass through a continuous first feeding device, making the desulfurization and denitrification additive pass through a continuous second feeding device, and respectively entering the reactor (2-1) of the regeneration simulation reaction unit, and contacting with the reaction gas to carry out the regeneration reaction, obtaining the regenerated flue gas and the regenerated agent; collecting and analyzing the regenerated flue gas to obtain the composition of the regenerated flue gas; and evaluating the performance of the desulfurization and denitrification additive according to the pollutant concentration in the composition of the regenerated flue gas. Continuous steady-state operation can be realized; it is more close to the actual industrial device to be built in a small and medium-sized laboratory; the operation is simple and accurate; and the mass ratio of the desulfurization and denitrification additive can also be changed under the same regeneration condition.

Description

Technical Field

[0001] This disclosure relates to the petrochemical field, specifically to a method and system for evaluating the performance of desulfurization and denitrification aids for continuous catalytic cracking flue gas. Background Technology

[0002] As an important resource, over 80% of petroleum products are used as fuel, providing energy and power for industries such as industry, agriculture, and transportation; the remainder serves as an important chemical raw material, driving the development of industries such as food, agriculture, pharmaceuticals, and daily chemicals.

[0003] Fluidized catalytic cracking (FCC) units are the core of the oil refining process, producing an estimated 45% of the world's gasoline. The core process is reaction regeneration, where the reaction itself primarily involves refining the various products; the regeneration process burns off the deactivated catalyst to regenerate it, while simultaneously providing the heat needed to maintain the reaction temperature. However, catalyst regeneration also generates significant amounts of polluting gases, including CO2, CO, and SO2. X and NO X NO X Emissions account for NO in the entire oil refining process X 50% of emissions. Therefore, controlling NO emissions during the catalytic cracking regeneration process is crucial. X and SO X Emissions are of great significance. The use of desulfurization and denitrification additives is particularly important for reducing NOx emissions from catalytic cracking regeneration flue gas. X and / or SO X The emissions are highly effective. Currently, there are generally two methods for evaluating the effectiveness of desulfurization and denitrification aids for catalytic cracking regeneration flue gas.

[0004] One operating method involves loading an evaluation target agent into the reactor. The target agent can be a mixture of desulfurization and denitrification aids and quartz sand in a certain proportion, adjusting the gas concentration to be similar to the target flue gas, and then starting the experiment. A method for evaluating the performance of an FCC regenerated flue gas desulfurization and denitrification catalyst disclosed in CN107029782A belongs to this type of operation. This evaluation method has two problems. First, the gas introduced into the reaction is pre-mixed flue gas, but in actual industrial production, flue gas does not exist directly in its final form; many reaction processes and intermediates still exist. This evaluation method, which directly uses the final flue gas products to evaluate the desulfurization and denitrification aids, is obviously different from reality. Another problem is that the experiment can only change the gas or temperature at a time, and cannot adjust the mixing ratio of the desulfurization and denitrification aids. If the reagent mixing ratio needs to be adjusted, the device needs to be shut down, cooled, cleaned, and refilled, and then the experiment needs to be restarted, consuming a lot of time.

[0005] Another method involves mixing the target agent with the pre-regeneration agent and then loading it into a reactor for experimentation. The introduced gas can be either coke air or a pre-mixed reaction gas. This method seems to solve the first problem mentioned above, using the coking process of the pre-regeneration agent instead of flue gas. However, this intermittent regeneration operation still differs from the continuous steady state of industrial regeneration. For example, in an intermittent evaluation device disclosed in CN104845661A, the flue gas component concentration over time exhibits a peak-like pattern, which differs from the steady state of the actual regeneration process. Furthermore, this method also faces the second problem mentioned above: the experimental operation of changing the catalyst mass concentration is cumbersome.

[0006] In addition, the continuous feed and discharge structure used in industrial regenerators is mostly controlled by system differential pressure and slide valve. This structure is suitable for large-scale equipment, but in small-scale equipment, it faces the problems of complex control and easy wear of valve components. Furthermore, in industrial equipment, regardless of the discharge form, the conveying is basically carried out in the form of "full pipe flow", but when applied to small laboratory equipment, blockage is very likely to occur.

[0007] Furthermore, the mechanism of action of desulfurization and denitrification additives within the reactor has always been an important research direction. However, current experimental setups mostly detect the components of the reaction tail gas, making it difficult to conduct in-depth research on the desulfurization and denitrification reaction process. A few processes attempt to sample by opening holes on the side of the reactor, but the number of holes is still limited by the reactor manufacturing process, and the accuracy is not high. Summary of the Invention

[0008] The purpose of this disclosure is to provide a method and system for evaluating the performance of desulfurization and denitrification aids in continuous catalytic cracking flue gas, which can achieve continuous steady-state operation; is suitable for building in small and medium-sized laboratories and is closer to actual industrial plants; is easy to operate and provides accurate evaluation; and allows for changing the mass ratio of desulfurization and denitrification aids under the same regeneration conditions.

[0009] To achieve the above objectives, the first aspect of this disclosure provides a method for evaluating the performance of a continuous catalytic cracking flue gas desulfurization and denitrification aid. The method includes the following steps: feeding the main agent to be generated into the reactor of a regeneration simulation reaction unit via a continuous first feeding device and feeding the desulfurization and denitrification aid via a continuous second feeding device, respectively, and contacting the reaction gas to carry out a regeneration reaction, thereby obtaining regenerated flue gas and regenerator.

[0010] The regenerated flue gas is collected and analyzed to obtain its composition; the performance of the desulfurization and denitrification aid is evaluated based on the pollutant concentrations in the regenerated flue gas composition.

[0011] Optionally, the method further includes: controlling the mass ratio of the main agent to the desulfurization and denitrification aid entering the reactor to multiple different preset mass ratios by adjusting the first feeding speed of the first feeding device for conveying the main agent and / or adjusting the second feeding speed of the second feeding device for conveying the desulfurization and denitrification aid; when the mass ratio of the main agent to the desulfurization and denitrification aid is adjusted to each preset mass ratio, obtaining the composition of the regenerated flue gas obtained from the regeneration reaction in the reactor under the preset mass ratio condition; then evaluating the performance of the desulfurization and denitrification aid in the regeneration reaction under the preset mass ratio condition based on the pollutant concentration in the regenerated flue gas composition obtained under each preset mass ratio condition; optionally, the lower the pollutant concentration in the regenerated flue gas composition, the better the performance of the desulfurization and denitrification aid under the mass ratio condition; preferably, in the process of obtaining the composition of the regenerated flue gas under each preset mass ratio condition, the method further includes: acquiring multiple CO2 concentration data in the regenerated flue gas under the preset mass ratio condition within a preset first acquisition and analysis period; then, based on the first concentration standard deviation σ of the multiple CO2 concentration data obtained, the method further includes: acquiring multiple CO2 concentration data in the regenerated flue gas under the preset mass ratio condition; and then evaluating the performance of the desulfurization and denitrification aid under the preset mass ratio condition based on the first concentration standard deviation σ of the acquired multiple CO2 concentration data. CO2 Determine whether the pollutant composition in the regenerated flue gas under the preset mass ratio condition has reached a steady state; optionally, the preset first collection and analysis cycle time is 1 to 20 seconds, preferably 1 to 5 seconds; optionally, when the first concentration standard deviation σ CO2 When the concentration is below 0.5%, preferably below 0.2%, the pollutant composition in the regenerated flue gas reaches a steady state under the preset mass ratio condition; preferably, the first concentration standard deviation σ CO2 The number of CO2 concentration data required for calculation is 10 to 60, preferably 20 to 40. When the pollutant composition in the regenerated flue gas under the preset mass ratio condition reaches a steady state, the composition of the regenerated flue gas after the steady state is taken as the composition of the regenerated flue gas under the preset mass ratio condition.

[0012] Optionally, the method further includes: feeding the main agent into the reactor via a continuous first feeding device and contacting it with the reaction gas to undergo a regeneration reaction, obtaining blank group regenerated flue gas and blank group regenerator; collecting and analyzing the blank group regenerated flue gas to obtain the composition of the blank group flue gas; evaluating the performance of the desulfurization and denitrification aid under the preset mass ratio condition based on the difference in pollutant concentration between the regenerated flue gas obtained by the regeneration reaction in which the desulfurization and denitrification aid was introduced at the preset mass ratio and the blank regenerated flue gas; preferably, the greater the difference in pollutant concentration between the regenerated flue gas and the blank regenerated flue gas, the better the performance of the desulfurization and denitrification aid under the preset mass ratio condition.

[0013] Optionally, before step S1, the method further includes a steady-state experiment preparation step; optionally, the steady-state experiment preparation step includes: pre-setting a balancing agent in the reactor, then allowing the regenerator to enter the reactor through the continuous first feeding device, contacting the reactant gas to carry out a regeneration reaction, obtaining steady-state prepared regeneration flue gas and steady-state prepared regenerator; displacing the balancing agent by discharging it through the reactor outlet; leading the steady-state prepared regeneration flue gas out through the reactor flue gas outlet, and discharging the steady-state prepared regenerator through the reactor outlet; acquiring multiple CO2 concentration data in the steady-state prepared regeneration flue gas within a preset second acquisition and analysis period; and then calculating the second concentration standard deviation σ of the multiple steady-state prepared regeneration flue gas data. CO2 'Determine whether the composition of pollutants in the prepared flue gas has reached a steady state; optionally, the preset second collection and analysis cycle time is 1-20s, preferably 1-5s; preferably, the second concentration standard deviation σ...' CO2 The number of CO2 concentration data points required for calculation is 10 to 60, preferably 20 to 40; optionally, when the second concentration standard deviation σ CO2 The concentration is below 0.5%, preferably below 0.2%, to ensure that the composition of pollutants in the regenerated flue gas reaches a steady state.

[0014] Optionally, the feeding unit includes a first feeding device, a second feeding device, and a feed riser; the method further includes: conveying the main agent to the feed riser via the first feeding device, and then into the reactor; conveying the desulfurization and denitrification aid via the second feeding device to the feed riser, and then into the reactor; optionally, a regenerator outlet is provided on the side wall of the reactor, and a discharge riser is connected to the outside of the regenerator outlet; the method further includes: allowing the solid particles in the reactor to overflow into the discharge riser via the regenerator outlet on the side wall of the reactor; and then flowing out of the reactor via the discharge riser into the regenerator recovery and analysis unit; optionally, the solid particles include regenerator and desulfurization and denitrification aid; optionally, the method includes: allowing the solid particles in the reactor to flow out via the discharge riser and then be divided into two parts by a particle diversion valve; allowing one part of the solid particles to enter the regeneration storage bin, and allowing the other part of the solid particles to enter the particle sampling bottle.

[0015] Optionally, the reactor is axially provided with a flue gas sampling pipe penetrating the top of the reactor, and the flue gas sampling pipe is movable along the reactor axis; the port of the flue gas sampling pipe inside the reactor forms a flue gas sampling inlet, and the port of the flue gas sampling pipe outside the reactor forms a flue gas sampling outlet, the flue gas sampling outlet being used to connect to a flue gas composition detection device; the method further includes: moving the flue gas sampling pipe up and down along the reactor axis to collect regenerated flue gas samples obtained from reactions at different axial positions of the reactor bed; and performing the following on the regenerated flue gas samples collected at each position: allowing the regenerated flue gas samples to flow out of the reactor through the flue gas sampling outlet of the flue gas sampling pipe and be divided into two regenerated flue gas samples; allowing one regenerated flue gas sample to enter a flue gas sampling bag, and the other regenerated flue gas sample to enter a sampling flue gas analyzer to obtain the regenerated flue gas composition at that position.

[0016] Preferably, the axial height difference between two adjacent positions in different axial positions is 1–500 mm; the axial movement speed of the flue gas sampling tube from top to bottom or from bottom to top is 0.5–5 mm / s; preferably, 3–50 regenerated flue gas samples with different axial positions are selected; preferably, the method further includes: obtaining the pressure at each bed position of the regenerated flue gas sample through a pressure sensor; and then evaluating the bed pressure stability at different axial positions in the reactor based on the pressure of the regenerated flue gas samples at different axial positions.

[0017] Optionally, the reactor is provided with a gas distribution plate at the bottom, and the reactor is divided into a gas pre-distribution chamber and a reaction chamber by the gas distribution plate, with the gas pre-distribution chamber located below the reaction chamber; the method further includes: allowing the reaction gas to enter the gas pre-distribution chamber of the reactor sequentially through a pressure regulating valve, a gas flow meter, and a gas preheater; and then entering the reaction chamber of the reactor upwards through the gas distribution plate to contact the solid particles in the reactor; wherein the solid particles include the main agent and desulfurization and denitrification aid; preferably, the reaction gas is preheated to 10-300°C by the gas preheater before entering the gas pre-distribution chamber, preferably preheated to 100-250°C.

[0018] Optionally, when evaluating denitrification performance: the reactant has a carbon content of 0.5–3% by weight, a carbon-to-hydrogen molar ratio of 0.2–3, and a bulk density of 700–1000 kg / m³. 3 The particle density is 1200–1600 kg / m³ 3 The skeletal density is 2300–2800 kg / m³. 3Preferably, the regenerated flue gas obtained from the regeneration reaction has NO concentrations of 0–1000 ppm, NO2 concentrations of 0–1000 ppm, HCN concentrations of 0–1000 ppm, and NH3 concentrations of 0–1000 ppm. When evaluating desulfurization performance: the reactant has a carbon content of 0.5–3% by weight, a carbon-to-hydrogen molar ratio of 0.2–3, and a bulk density of 700–1000 kg / m³. 3 The particle density is 1200–1600 kg / m³ 3 The skeletal density is 2300–2800 kg / m³. 3 Preferably, the SO₂ in the regenerated flue gas obtained from the regeneration reaction is... X The concentration is 0–3000 ppm; the reaction gas is selected from one or more of air, oxygen, nitric oxide, ammonia, carbon monoxide, and nitrogen; preferably, the oxygen volume content in the reaction gas is 0–100% by volume, more preferably 21–40% by volume.

[0019] Optionally, the feeding rate of the desulfurization and denitrification aid is 0.001–20 g / s; the feeding rate of the main agent is 0.1–20 g / s; the mass ratio of the desulfurization and denitrification aid to the main agent in the reactor is 0.01–1:1, preferably 0.01–0.1:1; the reaction conditions in the reactor include: a temperature of 500–800℃, preferably 650–750℃; a pressure of 0–0.5 MPa, preferably 0.15–0.25 MPa; and an apparent gas velocity of 0.01–0.8 m / s, preferably 0.1–0.6 m / s.

[0020] The second aspect of this disclosure provides a continuous catalytic cracking flue gas desulfurization and denitrification aid performance evaluation system. The system includes: a feeding unit, a regeneration simulation reaction unit, a gas supply unit, a regeneration flue gas acquisition and analysis unit, and a regenerator recovery and analysis unit. The feeding unit includes a continuous first feeding device and a continuous second feeding device. The first feeding device includes a pre-regenerated main agent outlet, and the second feeding device includes a desulfurization and denitrification aid outlet. The regeneration simulation reaction unit includes a reactor, which includes a feed inlet, a reaction gas inlet, a regeneration flue gas outlet, and a regenerator outlet. The feed inlet is connected to the pre-regenerated main agent outlet of the first feeding device and the desulfurization and denitrification aid outlet of the second feeding device, respectively. The regeneration flue gas outlet is connected to the regeneration flue gas analysis and acquisition unit, and the regenerator outlet is connected to the regenerator recovery and analysis unit.

[0021] Optionally, the first and second feeding devices include feeding structures with identical structures; the feeding structure includes: a storage bin, a feeding screw, and an external pressure protective gas structure; the feeding screw includes an idle section, a feeding section, and a conveying section; the external pressure protective gas structure includes an external pressure protective gas shell, a pressing end cap, and a particle feeder shell, the external pressure protective gas shell is sleeved outside the idle section of the feeding screw, the pressing end cap is disposed at the end of the idle section, and the pressing end cap and the first end face of the external pressure protective gas shell are sealed by a protective gas shaft seal; there is a gap between the inner wall of the external pressure protective gas shell and the outer wall of the feeding screw to form an annular cavity around the feeding screw, and an inlet pipe and an outlet pipe are provided on the external pressure protective gas shell to connect the annular cavity to the gas source through the inlet pipe and to the external pressure protective gas through the outlet pipe. The shell is externally connected; optionally, the lateral length of the annular cavity is 0.5-8 mm; optionally, a pressure sensor and a control valve are provided on the air inlet pipe; a back pressure valve is provided on the air outlet pipe; the granular feeder shell is sleeved outside the feeding section of the feeding screw, and the first end face of the granular feeder shell and the second end face of the external pressure protective gas shell are sealed by a feeding shaft seal; wherein, the feeding screw outlet of the first feeding device forms the outlet of the main agent to be generated; the feeding screw outlet of the second feeding device forms the outlet of the desulfurization and denitrification auxiliary agent; optionally, the regeneration simulation reaction unit further includes a feeding riser; the inlet of the feeding riser is located outside the reactor, and the outlet of the feeding riser is located inside the reactor; the inlet of the feeding riser is connected to the outlet of the main agent to be generated and the outlet of the desulfurization and denitrification auxiliary agent of the feeding unit, respectively.

[0022] Optionally, the regenerated flue gas acquisition and analysis unit includes a flue gas sampling tube, a pressure sensor, a three-way valve, a flue gas sampling bag, and a sampling flue gas analyzer; the flue gas sampling tube is installed through the regenerated flue gas outlet at the top of the reactor; the opening of the flue gas sampling tube inside the reactor forms a flue gas sampling inlet, and the opening of the flue gas sampling tube outside the reactor forms a flue gas sampling outlet; and the flue gas sampling tube is configured to move axially up and down within the reactor to sample the regenerated flue gas at different axial positions of the reactor bed; preferably, a gas-sealing structure is provided at the position where the flue gas sampling tube communicates with the regenerated flue gas outlet of the reactor; the outlet of the flue gas sampling tube is connected to one opening of the three-way valve. Of the remaining two openings of the three-way valve, one is connected to the flue gas sampling bag, and the other is connected to the sampling flue gas analyzer. Preferably, the pressure sensor is located on the connecting pipeline between the outlet of the flue gas sampling tube and the three-way valve. Optionally, the regenerated flue gas collection and analysis unit further includes a cyclone separator, a tail gas analyzer, and a reactor back pressure valve. The flue gas inlet of the cyclone separator is located below the reactor bed, the flue gas outlet of the cyclone separator is located at the top of the reactor and is connected to the tail gas analyzer. The reactor back pressure valve is located on the connecting pipeline between the flue gas outlet of the cyclone separator and the tail gas analyzer to control the pressure inside the reactor by adjusting the opening of the reactor back pressure valve.

[0023] Optionally, the reactor is provided with a gas distribution plate at the bottom, dividing the reactor into an upper gas pre-distribution chamber and a lower reaction chamber. The reaction gas inlet is located at the bottom of the gas pre-distribution chamber. The gas supply unit includes a pressure regulating valve, a gas flow meter, and a gas preheater connected in sequence. The preheated reaction gas outlet of the gas preheater is connected to the reaction gas inlet of the gas pre-distribution chamber. The regenerant recovery and analysis unit includes a discharge riser, a particle diversion valve, a regenerated storage bin, a discharge valve, a particle sampling valve, and a particle sampling bottle. The discharge riser is located at the bottom of the reactor. The reactor is located outside the reactor, and the regenerant outlet of the reactor is connected to the upper inlet of the discharge riser so that the regenerant in the reactor overflows into the discharge riser; the lower outlet of the discharge riser is connected to the inlet of the particle diversion valve; the particle diversion valve includes a first diversion outlet and a second diversion outlet; the first diversion outlet is connected to the particle sampling bottle via the particle sampling valve; the second diversion outlet is connected to the inlet of the regenerated storage silo; the discharge valve is located on the outlet pipeline at the bottom of the regenerated storage silo; optionally, one or more heating devices are also provided outside the reactor.

[0024] Through the above technical solutions, this disclosure provides a continuous catalytic cracking flue gas desulfurization and denitrification aid performance evaluation method and system. This method can stably and continuously simulate the desulfurization and denitrification process of industrial regenerated flue gas desulfurization and denitrification aids. Utilizing a stable and effective experimental window, multiple data and sample collection and analysis operations can be performed at multiple points. Furthermore, this disclosure can change the proportion of the desulfurization and denitrification aid in the total catalyst by adjusting the output of the first and second feeding devices. This allows for the evaluation of the desulfurization and denitrification effects of the aid under different mass ratios in a near-actual industrial regeneration process test, making it closer to the actual industrial production process. Moreover, changing the mass ratio of the desulfurization and denitrification aid does not require disassembling the reactor for feeding and unloading, greatly shortening the evaluation time. Thus, with low cost and simple operation, the evaluation of the desulfurization and denitrification effects of the catalytic cracking regenerated flue gas desulfurization and denitrification aid can be completed in a more realistic production environment.

[0025] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0026] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings:

[0027] Figure 1 This is an exemplary structural diagram of a continuous catalytic cracking flue gas desulfurization and denitrification additive performance evaluation system provided in this disclosure;

[0028] Figure 2 This is a schematic diagram of an exemplary structure of the flue gas sampling tube in this disclosure;

[0029] Figure 3 This is an exemplary structural diagram of a cyclone separator in this disclosure;

[0030] Figure 4 This is an exemplary structural diagram of the feeding device disclosed herein;

[0031] Figure 5 This is an exemplary structural diagram of the feeding device disclosed herein;

[0032] Figure 6 This is a graph showing the relationship between the NO concentration in the regenerated flue gas and the axial height of the reactor in Embodiment 1 of this disclosure;

[0033] Figure 7 This is a graph showing the relationship between the NH3 removal rate and the mass ratio of the auxiliary agent in Example 1 of this disclosure;

[0034] Figure 8 This is a graph showing the relationship between the composition of regenerated flue gas and its change over time in Embodiment 1 of this disclosure;

[0035] Figure 9 This is a graph showing the relationship between the composition of regenerated flue gas and its change over time in Comparative Example 1 of this disclosure.

[0036] Explanation of reference numerals in the attached figures

[0037] 1-1. Main agent storage silo; 1-2. First feeding device; 1-3. Feed riser; 1-4. Additive storage silo; 1-5. Second feeding device; 1-6-1. Storage silo; 1-6-2. Feeding screw; 1-6-3. External pressure protective gas structure; 1-6-4. External pressure protective gas shell; 1-6-5. Pressing end cap; 1-6-6. Particle feeder shell; 1-6-7. Feeding shaft seal; 1-6-8. O-ring; 1-6-9. Bolt fasteners; 1-6-10. Air inlet pipe; 1-6-11. Protective gas shaft seal; 1-6-12. Air outlet pipe; 1-6-13. Solid preheater; 2-1. Reactor; 2-2. Heating furnace; 2-3. Cyclone separator; 2- 4. Gas distribution plate; 2-5. Gas pre-distribution chamber; 3-1. Discharge riser; 3-2. Particle diversion valve; 3-3. Regenerated storage bin; 3-4. Discharge valve; 3-5. Particle sampling valve; 3-6. Particle sampling bottle; 4-1. Pressure stabilizing valve; 4-2. Gas flow meter; 4-3. Gas preheater; 5-1. Flue gas sampling pipe; 5-2. Pressure sensor; 5-3. Three-way valve; 5-4. Flue gas sampling bag; 5-5. Sampling flue gas analyzer; 5-6. Tail gas flue gas analyzer; 5-7. Reactor back pressure valve; 5-8. Temperature sensor; 5-1-1. Flue gas sampling pipe; 5-1-2. Packing gland; 5-1-3. Sealing packing; 5-1-4. Particle filter head. Detailed Implementation

[0038] The specific embodiments of this disclosure will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this disclosure.

[0039] In this disclosure, unless otherwise stated, the terms "first," "second," etc., are used only to distinguish different components and do not imply any actual meaning such as the order of connection. In this disclosure, directional terms such as "upper," "lower," "top," and "bottom" generally refer to the upper and lower, top and bottom, of the device in its normal operating state.

[0040] The first aspect of this disclosure provides a method for evaluating the performance of desulfurization and denitrification aids for continuous catalytic cracking flue gas, the method comprising the following steps:

[0041] The main agent to be generated is fed into reactor 2-1 of the regeneration simulation reaction unit via a continuous first feeding device, and the desulfurization and denitrification auxiliary agent is fed into reactor 2-1 via a continuous second feeding device. They then come into contact with the reaction gas to carry out a regeneration reaction, resulting in regenerated flue gas and regenerator.

[0042] The regenerated flue gas is collected and analyzed to obtain its composition; the performance of the desulfurization and denitrification aid is evaluated based on the pollutant concentrations in the regenerated flue gas composition.

[0043] This disclosure provides a continuous performance evaluation method for desulfurization and denitrification aids in catalytic cracking flue gas. It allows for stable and continuous simulation of the desulfurization and denitrification process of industrial regenerated flue gas, enabling multiple data and sample collection and analysis operations at multiple points within a stable and effective experimental window. Furthermore, by adjusting the outputs of the first and second feeding devices, the proportion of the desulfurization and denitrification aid in the total catalyst can be changed. This allows for evaluation of the desulfurization and denitrification effects of the aid under different mass ratios in a near-actual industrial regeneration process, more closely resembling the actual industrial production process. Moreover, changing the mass ratio of the aid does not require disassembling the reactor for feeding and unloading, significantly shortening the evaluation time. Thus, with low cost and simple operation, the evaluation of the desulfurization and denitrification effects of the aid in catalytic cracking regenerated flue gas can be completed under conditions closer to actual production.

[0044] In one embodiment, the method further includes: controlling the mass ratio of the main agent to the desulfurization and denitrification aid entering the reactor 2-1 to a plurality of different preset mass ratios by adjusting the first feeding speed of the first feeding device for conveying the main agent and / or adjusting the second feeding speed of the second feeding device for conveying the desulfurization and denitrification aid;

[0045] When the mass ratio of the main agent to the desulfurization and denitrification auxiliary agent is adjusted to each preset mass ratio, the composition of the regenerated flue gas obtained by the regeneration reaction in reactor 2-1 under the preset mass ratio condition is obtained.

[0046] Then, based on the pollutant concentration in the regenerated flue gas composition obtained under each preset mass ratio condition, the performance of the desulfurization and denitrification aid in the regeneration reaction under that preset mass ratio condition is evaluated.

[0047] Optionally, the lower the concentration of pollutants in the regenerated flue gas composition, the better the performance of the desulfurization and denitrification aid under the given mass ratio conditions.

[0048] In this disclosure, the mass ratio of the pre-fermenting agent to the desulfurization and denitrification aid can be changed in a continuous evaluation reaction by adjusting the output (feeding rate) of the first and second feeding devices, without the need for shutdown and reinstallation, making the operation simpler and more controllable.

[0049] In this disclosure, the relationship between the feeding rate of the first and second feeding devices used in the evaluation process and the mass ratio of the main agent to the desulfurization and denitrification auxiliary agent can be predetermined before the evaluation test is conducted.

[0050] In this disclosure, after adjusting the mass ratio of the main regenerating agent to the desulfurization and denitrification aid in reactor 2-1, it is also necessary to use the composition of the regenerated flue gas after the regeneration reaction in reactor 2-1 reaches a steady state to improve the accuracy of the evaluation.

[0051] In one specific embodiment, the method further includes the following steps in obtaining the composition of the regenerated flue gas under each preset mass ratio condition:

[0052] Within a preset first data acquisition and analysis period, multiple CO2 concentration data in the regenerated flue gas under the preset mass ratio conditions are acquired; then, based on the first concentration standard deviation σ of the acquired multiple CO2 concentration data... CO2 Determine whether the composition of pollutants in the regenerated flue gas under the preset mass ratio condition has reached a steady state;

[0053] Once the pollutant composition in the regenerated flue gas reaches a steady state under the preset mass ratio conditions, the composition of the regenerated flue gas after reaching a steady state is taken as the composition of the regenerated flue gas under the preset mass ratio conditions. Using the method disclosed herein, it is possible to more accurately determine whether the regenerated flue gas has reached a steady state, thereby improving detection efficiency.

[0054] In a preferred embodiment, when the first concentration standard deviation σ CO2 When the concentration is below 0.5%, preferably below 0.2%, the pollutant composition in the regenerated flue gas reaches a steady state under the preset mass ratio condition.

[0055] In one specific embodiment, the preset first acquisition and analysis cycle time is 1 to 20 seconds, preferably 1 to 5 seconds;

[0056] Preferably, the first concentration standard deviation σ CO2 The number of CO2 concentration data points required for the calculation is 10 to 60, preferably 20 to 40.

[0057] In one specific embodiment, the regenerated flue gas composition under each preset mass ratio condition is the exhaust gas obtained after separation by cyclone separator 2-3, and then detected by exhaust gas analyzer 5-6. This disclosure uses cyclone separator 2-3 to separate the regenerated flue gas, which can avoid the inclusion of solid impurities in the regenerated flue gas.

[0058] In a further embodiment, the method further includes: feeding the main agent to be regenerated into reactor 2-1 via a continuous first feeding device, and contacting it with the reaction gas to carry out a regeneration reaction, thereby obtaining blank group regenerated flue gas and blank group regenerator; collecting and analyzing the blank group regenerated flue gas to obtain the composition of the blank group flue gas;

[0059] The performance of the desulfurization and denitrification aid under the preset mass ratio is evaluated based on the difference in pollutant concentration between the regenerated flue gas obtained by the regeneration reaction in which the desulfurization and denitrification aid is introduced at the preset mass ratio and the blank regenerated flue gas. Preferably, the greater the difference in pollutant concentration between the regenerated flue gas and the blank regenerated flue gas, the better the performance of the desulfurization and denitrification aid under the preset mass ratio.

[0060] In a preferred embodiment, the method further includes a steady-state experiment preparation step before step S1.

[0061] In one specific embodiment, the steady-state experiment preparation steps include:

[0062] A balancing agent is pre-set in the reactor 2-1, and then the regenerating agent is fed into the reactor 2-1 through the continuous first feeding device to regenerate in contact with the reaction gas to obtain steady-state ready-to-regenerate flue gas and steady-state ready-to-regenerate agent; and the balancing agent is discharged through the outlet of the reactor 2-1 to replace the balancing agent.

[0063] The steady-state preparation regeneration flue gas is led out through the flue gas outlet of reactor 2-1, and the steady-state preparation regeneration agent is discharged through the discharge port of reactor 2-1;

[0064] Within the preset second data acquisition and analysis period, multiple steady-state CO2 concentration data in the prepared regeneration flue gas are acquired; then, based on the second concentration standard deviation σ of the multiple steady-state prepared regeneration flue gas CO2 concentration data... CO2 'Determine whether the composition of pollutants in the prepared flue gas has reached a steady state; optionally, the preset second collection and analysis cycle time is 1-20s, preferably 1-5s; preferably, the second concentration standard deviation σ...' CO2 The number of CO2 concentration data points required for the calculation is 10 to 60, preferably 20 to 40.

[0065] Optionally, when σ CO2 The concentration is below 0.5%, preferably below 0.2%, to ensure that the composition of pollutants in the regenerated flue gas reaches a steady state.

[0066] This disclosure describes a steady-state preparation of the regeneration reaction within reactor 2-1 using a displacement method (replacing the balancing agent with the regenerating agent). After starting the experimental setup, the apparatus is adjusted to ensure that key parameters during the evaluation process, including reaction temperature, pressure, apparent gas velocity, particle feed rate, bed stock, particle overflow velocity, gas residence time, and solid residence time, meet the evaluation requirements (pre-determined before the evaluation experiment). The second standard deviation σ of the CO2 concentration data in the multiple steady-state prepared regeneration flue gas in reactor 2-1 is used as the benchmark. CO2The concentration is below 0.5%, preferably below 0.2%, indicating that the equilibrium agent originally laid in reactor 2-1 has been completely replaced, the bed fluidization and reaction state in reactor 2-1 are stable, and subsequent steady-state evaluation experiments can be started.

[0067] In one specific embodiment, the steady-state preparation includes the following steps:

[0068] a. The reaction gas is preheated to a first temperature by the gas preheater 4-3 and then enters the reactor 2-1; the pressure inside the reactor 2-1 is controlled to the target pressure by adjusting the opening of the reactor back pressure valve 5-7; optionally, the first temperature of the reaction gas is 10-300℃, preferably 100-250℃; the target pressure is 0-0.5MPa, preferably 0.15-0.25MPa; the apparent gas velocity of the reaction gas is 0.01-0.8m / s, preferably 0.1-0.6m / s;

[0069] b. After the balancing agent is fed into the reactor 2-1 through the first feeding device to the target level, the feeding of the balancing agent is stopped; the target level of the balancing agent is preferably 1.2 to 1.7 times the bed level of the reactor 2-1;

[0070] c. The main agent to be generated is fed into the reactor 2-1 through the first feeding device, and it comes into contact with the reaction gas to undergo a third regeneration reaction, thereby obtaining steady-state pre-regeneration flue gas and steady-state pre-regeneration agent; the balance agent in the reactor 2-1 overflows into the outlet of the discharge riser 3-1 and flows out of the reactor 2-1.

[0071] The temperature inside the reactor 2-1 is controlled to a second target temperature; optionally, the second target temperature is 500-800℃, preferably 650-750℃;

[0072] d. The steady-state preparation regeneration flue gas is separated by cyclone separator 2-3 and then flows out, and the composition of the steady-state preparation regeneration flue gas is obtained by tail gas flue gas analyzer 5-6; the steady-state preparation regenerator flows out through discharge riser 3-1 and enters particle sampling bottle 3-6 to obtain the carbon content of the steady-state preparation regenerator.

[0073] The specific process flow for the steady-state preparation step in this disclosure includes: pre-placing a sufficient amount of balancing agent in reactor 2-1; connecting the reaction gas inlet gas path to the gas source required for the evaluation reaction in the evaluation operation; turning on all instruments; heating furnace 2-2 and gas preheater 4-3 to raise the temperature; then replacing the balancing agent pre-placed in reactor 2-1, including: introducing reaction gas into reactor 2-1, adjusting the opening of reactor back pressure valve 5-7 and the output power of heating furnace 2-2, so that the temperature, pressure, particle mass flow rate, and gas flow rate in reactor 2-1 all reach predetermined values; closing the first feeding device, the second feeding device, and the reaction gas path; then adding the main agent to be generated into main agent storage silo 1-1, and adding the desulfurization and denitrification aid into aid storage silo 1-4. The experiment is initiated, allowing the main agent to enter reactor 2-1 via the first feeding device. The reaction gas required for the evaluation reaction is sequentially distributed to the bottom of reactor 2-1 via pressure stabilizing valve 4-1, gas flow meter 4-2, and gas preheater 4-3, then uniformly distributed by gas distribution plate 2-4. The reaction gas flows upwards, contacting the main agent for regeneration. With the continuous introduction of the main agent, solid particles within reactor 2-1 overflow from the outlet on the side wall of reactor 2-1 into the discharge riser 3-1, where they are collected and analyzed. The regenerated flue gas is separated by cyclone separator 2-3 at the top of reactor 2-1 and then analyzed by exhaust gas analyzer 5-6. During this process, the gas velocity of the reaction gas, the feeding rate of the first feeding device, and the temperature within reactor 2-1 are adjusted according to the instruments. After a period of feeding, the exhaust gas analyzer 5-6 displays a stable composition (i.e., the second concentration standard deviation σ). CO2 The presence of 0.5% or less, and the stable carbon and sulfur content of the main agent in the regenerated storage silo, indicates that the balance agent originally laid in reactor 2-1 has been completely replaced, the bed fluidization and reaction state in reactor 2-1 are stable, and steady-state preparation is complete.

[0074] In one embodiment, the feeding unit includes a first feeding device, a second feeding device, and a feed riser 1-3; the method further includes:

[0075] The main agent to be produced is fed into the feed riser 1-3 by the first feeding device, and then enters the reactor 2-1; the desulfurization and denitrification aid is fed into the feed riser 1-3 by the second feeding device, and then enters the reactor 2-1.

[0076] Optionally, the reactor 2-1 has a regenerant outlet on its side wall, and a discharge riser 3-1 is connected to the outside of the regenerant outlet; the method further includes:

[0077] Solid particles within reactor 2-1 overflow through the regenerant outlet on the side wall of reactor 2-1 into the discharge riser 3-1; then, they flow out of reactor 2-1 through the discharge riser 3-1 into the regenerant recovery and analysis unit. Optionally, the solid particles include regenerant and desulfurization and denitrification aids. The discharge method of reactor 2-1 in this disclosure is simple and more suitable for small-scale equipment, avoiding problems such as complex control and easy wear of valves. Furthermore, this disclosure uses a "non-full-pipe flow" discharge method, reducing the occurrence of clogging problems.

[0078] In one embodiment, the method includes: allowing solid particles in the reactor 2-1 to flow out through the discharge riser 3-1 and then being divided into two parts by a particle diversion valve 3-2; then, allowing one part of the solid particles to enter the regeneration storage bin 3-3, and the other part of the solid particles to enter the particle sampling bottle 3-6. The outflowing regenerant can be sampled at any time through the particle diversion valve 3-2.

[0079] In one embodiment, a flue gas sampling pipe 5-1 is axially arranged through the top of the reactor 2-1, and the flue gas sampling pipe 5-1 is movable along the axial direction of the reactor 2-1; the opening of the flue gas sampling pipe 5-1 inside the reactor 2-1 forms a flue gas sampling inlet, and the opening of the flue gas sampling pipe 5-1 outside the reactor 2-1 forms a flue gas sampling outlet, the flue gas sampling outlet being used to connect to a flue gas composition detection device; the method further includes:

[0080] The flue gas sampling tube 5-1 is moved up and down along the axial direction of the reactor 2-1 to obtain regenerated flue gas samples obtained from different axial positions of the bed in the reactor 2-1.

[0081] The regenerated flue gas samples collected at each location are processed as follows: the regenerated flue gas samples flow out of the reactor 2-1 through the flue gas sampling outlet of the flue gas sampling tube 5-1 and are divided into two regenerated flue gas samples; one regenerated flue gas sample enters the flue gas sampling bag 5-4 and the other regenerated flue gas sample enters the sampling flue gas analyzer 5-5 to obtain the composition of the regenerated flue gas at that location.

[0082] Then, the regeneration reaction stability of the bed at different axial positions within the reactor 2-1 is evaluated based on the composition of the regenerated flue gas samples from different axial positions. In this disclosure, regenerated flue gas sampling at different bed positions can be achieved by axially moving the flue gas sampling tube 5-1. The method is simple and easy to control; and it eliminates the need for openings in the sidewall of reactor 2-1, making it more suitable for small-scale experimental devices. Additionally, two devices are provided: a flue gas sampling bag 5-4 and a flue gas analyzer 5-5. The choice can be made according to actual needs. For example, when a faster and simpler method is required but lower accuracy is needed, the flue gas analyzer 5-5 can be used. When higher accuracy is required or flue gas samples need to be preserved, the flue gas sampling bag 5-4 can be used to collect the flue gas for precise analysis or preservation using an instrument; or both methods can be used simultaneously.

[0083] In a preferred embodiment, the axial height difference between two adjacent positions in different axial positions is 1 to 500 mm; the axial movement speed of the flue gas sampling tube 5-1 from top to bottom or from bottom to top is 0.5 to 5 mm / s; preferably, 3 to 50 regenerated flue gas samples with different axial positions are selected.

[0084] In one embodiment, the method further includes: obtaining the pressure at each bed position using a pressure sensor from a regenerated flue gas sample at each location; and then evaluating the stability of the bed pressure at different axial positions within the reactor 2-1 based on the pressure of the regenerated flue gas samples at different axial positions. This disclosure also enables monitoring of the pressure at different bed positions within the reactor 2-1, allowing for timely adjustments after pressure fluctuations occur, which is beneficial for maintaining pressure stability within the reactor 2-1.

[0085] In one embodiment, a gas distribution plate 2-4 is provided at the lower part of the reactor 2-1, and the reactor 2-1 is divided into a gas pre-distribution chamber 2-5 and a reaction chamber by the gas distribution plate 2-4, with the gas pre-distribution chamber 2-5 located below the reaction chamber; the method further includes:

[0086] The reaction gas is sequentially introduced into the gas pre-distribution chamber 2-5 of the reactor 2-1 via the pressure regulating valve 4-1, the gas flow meter 4-2, and the gas preheater 4-3; then it enters the reaction chamber of the reactor 2-1 upwards via the gas distribution plate 2-4, and comes into contact with the solid particles in the reactor 2-1; wherein the solid particles include one or more of the main regenerator, desulfurization and denitrification aid, first regenerator and second regenerator, which is beneficial to improve the uniformity of the reaction gas distribution and make the contact between the reaction gas and the particles in the reactor 2-1 more uniform.

[0087] Preferably, the reaction gas is preheated to 10-300°C by a gas preheater 4-3, and then preheated to 100-250°C.

[0088] In one specific embodiment, the gas distribution plate 2-4 is provided with a plurality of evenly distributed gas distribution holes of uniform size and position. Optionally, the gas distribution plate 2-4 is made of a metal sintered plate or a ceramic sintered plate. Preferably, the filtration accuracy of the gas distribution plate 2-4 is 0.5-10 μm, and more preferably 0.5-5 μm. In this disclosure, the filtration accuracy of the gas distribution plate is as conventionally understood in the art.

[0089] In one embodiment, when evaluating denitrification performance: the reactant has a carbon content of 0.5–3% by weight, a carbon-to-hydrogen molar ratio of 0.2–3, and a bulk density of 700–1000 kg / m³. 3 The particle density is 1200–1600 kg / m³ 3 The skeletal density is 2300–2800 kg / m³. 3 Preferably, the NO concentration in the regenerated flue gas obtained from the regeneration reaction is 0-1000 ppm, the NO2 concentration is 0-1000 ppm, the HCN concentration is 0-1000 ppm, and the NH3 concentration is 0-1000 ppm.

[0090] When evaluating desulfurization performance: the carbon content of the pre-fermentation agent should be 0.5–3% by weight, the carbon-hydrogen molar ratio should be 0.2–3, and the bulk density should be 700–1000 kg / m³. 3 The particle density is 1200–1600 kg / m³ 3 The skeletal density is 2300–2800 kg / m³. 3 Preferably, the SO₂ in the regenerated flue gas obtained from the regeneration reaction is... X Concentration range: 0–3000 ppm;

[0091] The reaction gas is selected from one or more of air, oxygen, nitric oxide, ammonia, carbon monoxide, and nitrogen; preferably, the oxygen content in the reaction gas is 0-100% by volume, more preferably 21-40% by volume.

[0092] In this disclosure, the particle density of the regenerating agent is measured using a mercury porosimeter.

[0093] In one embodiment, the feeding rate of the desulfurization and denitrification aid is 0.001–20 g / s, preferably 0.02 g / s; the feeding rate of the pre-fermentation main agent is 0.1–20 g / s, preferably 1.98 g / s; the mass ratio of the desulfurization and denitrification aid to the pre-fermentation main agent in reactor 2-1 is 0.01–1:1, preferably 0.01–0.1:1;

[0094] The reaction conditions in reactor 2-1 include: a temperature of 500–800℃, preferably 650–750℃; a pressure of 0–0.5 MPa, preferably 0.15–0.25 MPa; and an apparent gas velocity of 0.01–0.8 m / s, preferably 0.1–0.6 m / s.

[0095] In one specific embodiment, the method further includes pretreatment of the particles and gases required for the evaluation test, comprising the following steps:

[0096] Select the required particles (including the main catalyst and desulfurization and denitrification aids) and reaction gas according to the industrial equipment to be evaluated; perform screening, conditioning, heating, drying, aging, and contamination treatments on the required main catalyst and desulfurization and denitrification aids; pre-calculate the mass ratio of each aid to be evaluated in the total catalyst; calibrate the feeding rate of the first feeding device for the main catalyst and the second feeding device for the desulfurization and denitrification aids, and determine the control coefficient (i.e., the ratio of feeding rate to output speed) to facilitate precise control and accurate results in subsequent evaluation experiments; adjust the composition of the reaction gas required for the reaction, and adjust the reaction gas in the evaluation experiment according to the evaluation requirements (including four evaluation criteria: evaluation of desulfurization effect of conventional regeneration operation, evaluation of high denitrification requirement, evaluation of desulfurization effect of conventional regeneration operation, and evaluation of high desulfurization requirement).

[0097] In this disclosure, the concentration of pollutant components in the regenerated flue gas obtained from the blank experimental group (the regeneration reaction of the pre-regenerated agent when the mass percentage of the desulfurization and denitrification additive is 0% by weight) is denoted as W0; the concentration of pollutant components in the regenerated flue gas obtained from the regeneration reaction using the same pre-regenerated agent when the mass percentage of the desulfurization and denitrification additive is i% by weight (based on the total weight of the additive and the pre-regenerated agent) is denoted as W0. i The removal rate T is calculated using the following formula (1). i (%) is the performance evaluation index of desulfurization and denitrification aids when the aid mass percentage is i% by weight:

[0098] T i (%) = (W0 - W) i Equation (1) is: ) / W0×100%.

[0099] The pollutant components include nitrogen-containing and sulfur-containing compounds, such as NH3 and SO2, which can be selected according to the evaluation requirements. The removal rate of each pollutant component is calculated using formula (1).

[0100] In the first specific implementation, when evaluating the denitrification effect of conventional regeneration operation, the reaction gas is air. The flow rate of the reaction gas can be adjusted according to the excess oxygen content of the target regeneration flue gas and the mass flow rate of the pre-regeneration agent. The excess oxygen content in the target regeneration flue gas is 2-10% by volume, and the mass flow rate of the pre-regeneration agent is 0.1-6 g / s. A blank experimental group is used when the mass percentage of the denitrification aid is 0% by weight. Then, experiments are conducted with different mass concentrations of denitrification aids. The NH3 concentration in the flue gas is measured, the removal rate is calculated, and the denitrification effect is evaluated. Among them, when the NH3 removal rate in the regeneration flue gas analysis results is greater than 90%, the denitrification effect is good; when the removal rate is 60-90%, the denitrification effect is relatively good; when the removal rate is 30-60%, the denitrification effect is average; and when the removal rate is less than 30%, the denitrification effect is poor.

[0101] In the second specific implementation, when evaluating high denitrification requirements, the reaction gas is selected from one or more of air, O2, N2, and NH3. Each component is pre-proportioned according to the target flue gas composition. The NH3 concentration in the reaction gas is 0–2000 ppm, preferably 800 ppm. Flue gas analysis results show that a denitrification effect is good when the NH3 removal rate is greater than 90%, relatively good when the NH3 removal rate is 60–90%, moderate when the removal rate is 30–60%, and poor when the NH3 removal rate is less than 30%.

[0102] In the third specific implementation, when evaluating the desulfurization effect of conventional regeneration operation, the reaction gas is air. The flow rate of the reaction gas can be adjusted according to the excess oxygen content in the target regeneration flue gas and the mass flow rate of the pre-regeneration agent. The excess oxygen content in the target regeneration flue gas is 2-10%, and the mass flow rate of the pre-regeneration agent is 0.1-6 g / s. Taking the desulfurization aid mass concentration of 0% by weight as a blank experimental group, experiments are conducted with different desulfurization aid mass concentration ratios. The SO2 concentration in the flue gas is measured, the removal rate is calculated, and the desulfurization effect is evaluated. In the flue gas analysis results, an SO2 removal rate greater than 95% is excellent, a removal rate of 80-95% is good, a removal rate of 70-80% is average, and a removal rate less than 70% is poor.

[0103] In the fourth specific implementation, when evaluating the high desulfurization demand, the reaction gas is selected from one or more of air, N2, and SO2; each component is pre-proportioned according to the target flue gas composition, and the SO2 concentration in the reaction gas composition is 0-3000 ppm, preferably 1500 ppm; the SO2 concentration in the flue gas is measured, the removal rate is calculated, and the desulfurization effect is evaluated; in the flue gas analysis results, an SO2 removal rate greater than 95% is excellent, a removal rate of 80-95% is good, a removal rate of 70-80% is average, and a removal rate less than 70% is poor.

[0104] In a further embodiment, a movable flue gas sampling tube 5-1 is used to sample the changes in the composition of the regenerated flue gas at different axial positions within the reactor 2-1, and a desulfurization and denitrification process diagram (e.g., a diagram showing the relationship between pollutant concentration in the regenerated flue gas and axial height) is plotted to study the mechanism of action and provide guidance for scale-up applications. A carbon-sulfur analyzer and an organic element analyzer are used to analyze the carbon content of the pre-regenerating agent and the regenerating agent after regeneration to evaluate the effect of the additive on the regeneration coking effect. The amplitude and frequency of pressure fluctuations within the bed are calculated by processing the pressure data within the bed.

[0105] In one specific implementation, the following is adopted: Figure 1 The system shown in this disclosure, and the performance evaluation method for continuous catalytic cracking flue gas desulfurization and denitrification additives, includes the following steps:

[0106] First, pretreatment of the particles and gases required for the evaluation experiment is carried out: The corresponding main agent and reactant gas are selected according to the evaluation needs. The main agent and auxiliary agents undergo screening, conditioning, heating, drying, aging, and contamination treatment. The composition and flow rate of the reactant gas are proportioned according to the experimental requirements. Then, the steady-state experiment preparation steps are performed, until the bed fluidization and reaction state in reactor 2-1 are stable (i.e., the second concentration standard deviation σ). CO2 When the concentration is below 0.5%, steady-state evaluation experiments can begin.

[0107] Record the characteristic data of the blank group (i.e., only the pre-fermentation agent is added, without the desulfurization and denitrification additives), and record the data of the composition of the blank regenerated flue gas in the blank group; then, according to the relationship between the feeding rate and the mass ratio of the desulfurization and denitrification additives pre-calibrated in the evaluation experiment, increase the output rate of the second feeding device for the desulfurization and denitrification additives to increase the mass ratio of the desulfurization and denitrification additives in the total catalyst (total amount of pre-fermentation agent and additives) to reach the preset mass ratio. After the composition of the regenerated flue gas reaches a steady state under the preset mass ratio condition (i.e., the first concentration standard deviation σ), CO2The concentration of the additive is below 0.5%, and characteristic data (such as regenerated flue gas composition, regenerator carbon content, and bed pressure in reactor 2-1) are recorded. Then, by increasing the additive feeding rate, an evaluation experiment is conducted to determine the preset mass ratio of the next desulfurization and denitrification additive (the relationship between feeding rate and mass ratio can be calibrated before the evaluation experiment). If the evaluation work requires simulation and evaluation of other special operating conditions, the inlet gas composition can be changed after the mass ratio experiment, and characteristic data under that condition can be recorded. The characteristic data is obtained through gas sampling analysis and monitoring of parameters such as temperature and pressure using flue gas sampling pipes, flue gas analyzers, temperature sensors, and pressure sensors. Finally, the concentrations of various components in the regenerated flue gas, especially nitrogen- and sulfur-containing compounds such as NO, NO2, N2O, NH3, SO2, and SO3, were obtained using a tail gas analyzer to evaluate the desulfurization and denitrification effects of the additive. A movable sampling tube was used to sample the axial changes in flue gas composition within the reactor, and a desulfurization and denitrification process diagram was plotted. A carbon-sulfur analyzer and an organic element analyzer were used to analyze the carbon content before and after catalyst regeneration to evaluate the impact of the additive on the regeneration coke burning effect. Finally, the effect of the simulated catalytic cracking regeneration flue gas desulfurization and denitrification operation of the additive was evaluated by processing the bed pressure data and calculating the amplitude and frequency of bed pressure fluctuations.

[0108] The specific operations and parameters for each step have been described in detail above and will not be repeated here.

[0109] The second aspect of this disclosure provides a performance evaluation system for continuous catalytic cracking flue gas desulfurization and denitrification additives, such as... Figure 1 As shown, the system includes: a feeding unit, a regeneration simulation reaction unit, a gas supply unit, a regeneration flue gas acquisition and analysis unit, and a regenerator recovery and analysis unit;

[0110] The feeding unit includes a continuous first feeding device and a continuous second feeding device; the first feeding device includes a discharge port for the main agent to be produced, and the second feeding device includes a discharge port for the desulfurization and denitrification auxiliary agent;

[0111] The regeneration simulation reaction unit includes reactor 2-1, which includes a feed inlet, a reaction gas inlet, a regeneration flue gas outlet, and a regenerator outlet. The feed inlet is connected to the main agent outlet of the first feeding device and the desulfurization and denitrification auxiliary agent outlet of the second feeding device, respectively. The regeneration flue gas outlet is connected to the regeneration flue gas analysis and acquisition unit. The regenerator outlet is connected to the regenerator recovery and analysis unit.

[0112] In one specific implementation, such as Figure 1As shown, the shell of reactor 2-1 is a cylindrical structure. Preferably, the shell of reactor 2-1 comprises, from bottom to top, a first cylindrical section (dense phase section) of equal diameter, a second cylindrical section (transition section) of varying diameter, and a third cylindrical section (dilute phase section) of equal diameter, wherein the inner diameter of the first cylindrical section is larger than the inner diameter of the third cylindrical section; the inner diameter of the cross-section of the second cylindrical section gradually increases axially from bottom to top, preferably a frustum-shaped structure, wherein the top of the frustum-shaped structure has the largest cross-sectional diameter, which is equal to the inner diameter of the third cylindrical section, and the bottom has the smallest cross-sectional diameter, which is equal to the inner diameter of the first cylindrical section. Preferably, the regenerant outlet is located on the side wall of the second cylindrical section.

[0113] In one specific embodiment, the inner diameter of the first section of the reactor 2-1 is 40-80 mm and the height is 60-160 mm; the vertical height of the second section is 60-80 mm and the angle between the side wall and the central axis is 0-45°, preferably 10-30°; the inner diameter of the third section is 40-200 mm and the height is 100-400 mm.

[0114] In a preferred embodiment, such as Figure 1 As shown, one or more heating devices, such as a heating furnace 2-2, are also provided outside the reactor 2-1, which helps to heat the reactor 2-1 and maintain a stable bed temperature.

[0115] In one embodiment, the first and second feeding devices of the feeding unit include feeding structures with identical structures. For example... Figure 4 and Figure 5 As shown, the feeding structure includes a storage bin (the storage bin in the first feeding device is the main agent storage bin 1-1, and the storage bin in the second feeding device is the auxiliary agent storage bin 1-4), a feeding screw 1-6-2, and an external pressure protective gas structure 1-6-3; the feeding screw 1-6-2 includes an idle section, a feeding section, and a transmission section;

[0116] The feeding screw 1-6-2 is divided into a feeding section and a conveying section along the material flow direction. Preferably, the feeding screw 1-6-2 also includes an empty section set upstream of the feeding section, that is, an empty screw area is set between the feeding port of the feeding screw 1-6-2 and the motor end of the screw, instead of feeding directly at the motor end of the screw.

[0117] The external pressure protective gas structure 1-6-3 includes an external pressure protective gas housing 1-6-4, a clamping end cap 1-6-5, and a pellet feeder housing 1-6-6. The external pressure protective gas housing 1-6-4 is sleeved outside the empty section of the feeding screw 1-6-2, and the clamping end cap 1-6-5 is located at the end of the empty section. The clamping end cap 1-6-5 and the first end face of the external pressure protective gas housing 1-6-4 are sealed by a protective gas shaft seal 1-6-11. A gap exists between the inner wall of feed screw 1-6-2 and the outer wall of feed screw 1-6-2 to form an annular cavity around feed screw 1-6-2. An inlet pipe 1-6-10 and an outlet pipe 1-6-12, penetrating the inside and outside of the external pressure protective gas housing 1-6-4, are provided on the annular cavity so that it is connected to the gas source through inlet pipe 1-6-10 and to the outside of external pressure protective gas housing 1-6-4 through outlet pipe 1-6-12. Optionally, the lateral length of the annular cavity is 0.5–8 mm. In this disclosure, the lateral length of the annular cavity refers to its length along the length of the screw.

[0118] In one implementation, such as Figure 1 As shown, the feed screw outlet of the first feeding device is configured as the discharge port of the main agent to be produced; the feed screw outlet of the second feeding device is configured as the discharge port of the desulfurization and denitrification auxiliary agent.

[0119] Optionally, the regeneration simulation reaction unit further includes a feed riser 1-3; the inlet of the feed riser 1-3 is located outside the reactor 2-1, and the outlet of the feed riser 1-3 is located inside the reactor 2-1; the inlet of the feed riser 1-3 is connected to the outlet of the main agent and the outlet of the desulfurization and denitrification auxiliary agent of the feeding unit, respectively. In this disclosure, the outlets of the first feeding device and the second feeding device are both connected to the inlet of the feed riser 1-3 to convey materials into the reactor 2-1.

[0120] In one implementation, such as Figure 4 As shown, the air inlet pipe 1-6-10 of the external pressure protective gas structure is equipped with a pressure sensor and a first control valve; the air outlet pipe 1-6-12 is equipped with a back pressure valve, which can adjust the pressure inside the cavity; the pellet feeder housing 1-6-6 is sleeved outside the feeding section of the feeding screw 1-6-2, and the first end face of the pellet feeder housing 1-6-6 and the second end face of the external pressure protective gas housing 1-6-4 are sealed by the feeding shaft seal 1-6-7; the inlet end of the feed riser 1-3 is connected to the conveying section of the feeding screw 1-6-2.

[0121] This disclosure incorporates an external pressure protective gas structure 1-6-3 within the feeding screw 1-6-2. The technical principle of the external pressure protective gas structure 1-6-3 is as follows: a small-volume cavity combined with a trace amount of gas is used to obtain high pressure. This high-pressure gas micro-clusters externally seal the tiny gaps that appear on the rotating shaft of the automatic particle feeder (feeding screw) during operation, preventing gas leakage from the inside to the outside of the reaction system. This device not only prevents reaction gas leakage but also prevents dry, hot fine powder from entering the tiny pores of the sealing surface, thus preventing the aging and failure of the sealing material. Furthermore, due to the increased length of the conveying section, problems such as bridging, increased friction loss, particle compression, and increased particle wear occur during particle conveying. This disclosure utilizes the trace amount of gas flowing into the system through the external pressure protective gas structure to widen the particle spacing, increase material flowability, and improve conveying efficiency, effectively solving the problems caused by the increased length of the conveying end. The trace amounts of gas in the external pressure protective gas structure will not cause significant interference to the flow field and reactant concentration inside the reactor, and the impact of the external pressure protective gas structure can be ignored. The external pressure protective gas uses nitrogen or inert gas, which can ensure that the solid material will not be contaminated or reacted by gaseous components that diffuse or back up from downstream during the transportation and heating process.

[0122] The feeding screw in this disclosure, in conjunction with the external pressure protection gas structure installed at the coupling end, achieves the effect of stable material delivery from the feeding device into the reactor.

[0123] In one implementation, such as Figure 4 As shown, the feeding screw 1-6-2 also includes a feeding inlet and a feeding outlet, which are located in the pellet feeder housing 1-6-6. The feeding inlet is connected to the outlet of the storage silo, and the feeding outlet is connected to the inlet end of the feed riser 1-3. Along the material transmission direction of the feeding screw 1-6-2, the feeding inlet is located downstream of the shaft seal and is spaced from the shaft seal to form an empty section. Preferably, the length of the empty section of the feeding screw 1-6-2 is 50-300 mm. This disclosure leaves an empty section before the feeding area, which can reduce the temperature rise of the rotating shaft caused by the preheating of the conveying section and protect the flexible sealing material at the shaft seal. At the same time, the empty area can also play a buffering role in special situations of the device, such as blockage of the balance pipe, insufficient external pressure protection gas pressure, or other reasons causing the reactor pressure to be much greater than the automatic pellet feeder pressure, preventing backflow gas from carrying a large number of particles to directly impact the shaft seal and damage the sealing structure.

[0124] In one implementation, such as Figure 4As shown, a solid preheater 1-6-13 is fitted outside the conveying section of the feeding screw 1-6-2 to form a preheating section on the feeding screw 1-6-2. There is a gap between the preheating inlet end of the solid preheater 1-6-13 and the feeding inlet of the feeding screw 1-6-2, and the feeding outlet of the feeding screw 1-6-2 is located in the preheating section. By installing the solid preheater 1-6-13 outside the feeding screw 1-6-2, the reactant can be heated to the target temperature before entering the reactor, improving the reaction efficiency within the subsequent reactor and avoiding large temperature fluctuations inside the reactor, which is beneficial for steady-state simulation operation.

[0125] In one specific embodiment, the total length of the conveying section of the feeding screw 1-6-2 is 200-1000 mm. In this disclosure, the total length of the conveying section between the feeding inlet and the feeding outlet is relatively long, and the specific length can be adjusted according to the particle preheating requirements and the power of the heating furnace to maintain the final particle discharge temperature. Optionally, the first feeding device maintains the final discharge temperature of the main agent particles at 10-550°C; the second feeding device maintains the final discharge temperature of the desulfurization and denitrification aid particles at 10-550°C.

[0126] In a preferred embodiment, the idle section and conveying section of the feeding screw 1-6-2 have an inclination angle, preferably any inclination angle between -30° and 30°. In this disclosure, the inclination angle where the feeding outlet is higher than the feeding inlet is considered positive. The automatic feeding device (feeding screw) used in this disclosure is set with an inclination angle such that when conveying particles with good flowability, the conveying section is installed with an appropriate upward inclination (0-30°) to increase feeding stability; when conveying particles with poor flowability, it needs to be appropriately tilted downward (-30-0°) to increase flowability.

[0127] In one implementation, such as Figure 1 As shown, the regenerated flue gas acquisition and analysis unit includes a flue gas sampling tube 5-1, a pressure sensor 5-2, a three-way valve 5-3, a flue gas sampling bag 5-4, and a sampling flue gas analyzer 5-5;

[0128] The flue gas sampling pipe 5-1 is installed through the regenerated flue gas outlet at the top of the reactor 2-1; the pipe opening of the flue gas sampling pipe 5-1 inside the reactor 2-1 forms a flue gas sampling inlet, and the pipe opening of the flue gas sampling pipe 5-1 outside the reactor 2-1 forms a flue gas sampling outlet; and the flue gas sampling pipe 5-1 is configured to move axially up and down inside the reactor 2-1 to sample the regenerated flue gas at different axial positions of the bed inside the reactor 2-1.

[0129] The outlet of the flue gas sampling tube 5-1 is connected to one opening of the three-way valve 5-3; of the remaining two openings of the three-way valve 5-3, one is connected to the flue gas sampling bag 5-4, and the other is connected to the sampling flue gas analyzer 5-5; preferably, the pressure sensor 5-2 is installed on the connecting pipeline between the outlet of the flue gas sampling tube 5-1 and the three-way valve 5-3. This disclosure uses only one flue gas sampling tube 5-1 to sample the regeneration reaction flue gas in the bed at different axial heights, which is simple, fast, and can be operated during the continuous regeneration reaction process.

[0130] In this disclosure, conventional device structures in the art can be used to move the flue gas sampling tube 5-1 up and down, such as setting pulleys or other structures outside the reactor 2-1.

[0131] In one specific embodiment, a gas-sealing structure is provided at the location where the flue gas sampling pipe 5-1 connects to the reactor 2-1 via the regenerated flue gas outlet; such as Figure 2 As shown, the flue gas sampling pipe 5-1-1 axially penetrates the inside and outside of the reactor 2-1 shell; and a sealing packing 5-1-3 is provided in the gap at the connection between the flue gas sampling pipe 5-1-1 and the reactor 2-1; and a packing gland 5-1-2 is provided above the connection position; wherein, the top of the flue gas sampling pipe 5-1-1 in the reactor 2-1 is provided with a particle filter head 5-1-4 to prevent particles from entering the sampling pipe, and a temperature sensor 5-8 is also provided at the sampling end of the flue gas sampling pipe 5-1-1 to obtain the temperature at the bed position during regeneration flue gas sampling.

[0132] In one implementation, such as Figure 1 As shown, the regenerated flue gas acquisition and analysis unit also includes a cyclone separator 2-3, a tail gas analyzer 5-6, and a reactor back pressure valve 5-7. The flue gas inlet of the cyclone separator 2-3 is located below the bed of the reactor 2-1, and the flue gas outlet of the cyclone separator 2-3 is located at the top of the reactor 2-1 and is connected to the tail gas analyzer 5-6. The reactor back pressure valve 5-7 is installed on the connecting pipeline between the flue gas outlet of the cyclone separator 2-3 and the tail gas analyzer 5-6, and is used to control the pressure inside the reactor 2-1 by adjusting the opening of the reactor back pressure valve 5-7, thereby stabilizing the pressure inside the reactor 2-1.

[0133] In this disclosure, the cyclone separator 2-3 is a built-in cyclone separator with a conventional structure in the art. In one specific embodiment, the structure of the cyclone separator 2-3 is as follows: Figure 3As shown, the cyclone separator 2-3 comprises, from top to bottom, an upper section with an equal diameter (inner diameter of 11 mm), a transition section with a variable diameter, a first lower section with an equal diameter (inner diameter of 8 mm), and a second lower section with an equal diameter (inner diameter of 3.4 mm). The inner diameter of the upper section with an equal diameter is larger than that of the first lower section with an equal diameter, and the inner diameter of the first lower section with an equal diameter is larger than that of the second lower section with an equal diameter. The top of the first lower section with an equal diameter is connected to the bottom of the upper section with an equal diameter via a frustum-shaped connecting section, and the bottom of the first lower section with an equal diameter is connected to the top of the second lower section with an equal diameter via a frustum-shaped connecting section. The bottom opening of the first lower section with an equal diameter serves as a sampling port for exhaust gas. The top of the upper section with an equal diameter is equipped with a purified exhaust gas regeneration exhaust gas outlet pipe (inner diameter of 6 mm) and an exhaust gas outlet pipe containing impurities (inner diameter of 4 mm). The purified exhaust gas regeneration exhaust gas outlet pipe is used to connect with the back pressure valve 5-7 of the reactor, and the exhaust gas outlet pipe containing impurities is connected with the internal space of the reactor 2-1 shell.

[0134] In one implementation, such as Figure 1 As shown, a gas distribution plate 2-4 is provided at the bottom of the reactor 2-1. With the gas distribution plate 2-4 as the boundary, the reactor 2-1 is divided into a gas pre-distribution chamber 2-5 at the top and a reaction chamber at the bottom; the reaction gas inlet is located at the bottom of the gas pre-distribution chamber 2-5.

[0135] The gas supply unit includes a pressure regulating valve 4-1, a gas flow meter 4-2, and a gas preheater 4-3 connected in sequence; the preheated reaction gas outlet of the gas preheater 4-3 is connected to the reaction gas inlet of the gas pre-distribution chamber 2-5.

[0136] In one implementation, such as Figure 1 As shown, the regenerant recovery analysis unit includes a discharge riser 3-1, a particle diversion valve 3-2, a regenerative storage bin 3-3, a discharge valve 3-4, a particle sampling valve 3-5, and a particle sampling bottle 3-6.

[0137] The discharge riser 3-1 is located outside the reactor 2-1, and the regenerant outlet of the reactor 2-1 is connected to the upper inlet of the discharge riser 3-1 so that the regenerant in the reactor 2-1 overflows into the discharge riser 3-1; the lower outlet of the discharge riser 3-1 is connected to the inlet of the particle diversion valve 3-2; the particle diversion valve 3-2 includes a first diversion outlet and a second diversion outlet; the first diversion outlet is connected to the particle sampling bottle 3-6 via the particle sampling valve 3-5; the second diversion outlet is connected to the inlet of the regenerated storage silo 3-3; the discharge valve 3-4 is located on the outlet pipeline at the bottom of the regenerated storage silo 3-3.

[0138] The process flow of each unit in the continuous catalytic cracking flue gas desulfurization and denitrification additive performance evaluation system provided in this disclosure has been described in detail above and will not be repeated here.

[0139] The technical solution of this disclosure will be specifically described below through specific embodiments.

[0140] In the following embodiments, the mass percentage of desulfurization and denitrification aids is based on the total mass of the desulfurization and denitrification aids.

[0141] Example 1

[0142] This implementation is used to evaluate the denitrification performance of conventional regeneration operations. Figures 1 to 5 The system shown.

[0143] The specific structure of the system includes: First, taking the first feeding device as an example, the feeding structure is explained. The second feeding device has the same structure as the first feeding device.

[0144] The specific structure of the system includes: a main agent storage silo 1-1 with a volume of 20L for the first feeding device; a feeding screw 1-6-2 arranged horizontally without any tilt angle; the screw thread is a rectangular thread machined from steel plate with a thread thickness of 1.5mm and a thread pitch of 20mm; the major diameter of the screw is 40mm and the minor diameter is 20mm; the feeding shaft seal 1-6-7 and the protective gas shaft seal 1-6-11 are made of polytetrafluoroethylene (PTFE); and the feeding screw... The lateral length of the unused section of 1-6-2 is 100mm, and the length of the conveying section is 600mm. The inner diameter of the inlet pipe 1-6-10 of the external pressure protective gas structure 1-6-3 is 4mm, and the outer diameter is 6mm. The inlet pipe 1-6-10 is connected to an argon cylinder and a gas quality controller. The outlet pipe 1-6-12 of the external pressure protective gas structure 1-6-3 is connected to an electrically controlled needle valve. The lateral length of the annular cavity of the external pressure protective gas structure 1-6-3 is 4mm. A solid preheater 1-6-13 is installed outside the conveying section of the feeding screw 1-6-2. The outlet of the conveying section and the outlet of the second feeding device are connected to the inlet end of the feeding riser 1-3.

[0145] The second feeding device has the same composition as the first feeding device, but some component dimensions differ. The additive storage silo has a volume of 5L. The feeding screw 1-6-2 is arranged horizontally without any tilt angle. The screw thread is a rectangular thread machined from steel plate, with a thread thickness of 1mm and a thread pitch of 10mm. The major diameter of the screw is 20mm, and the minor diameter is 10mm. The feeding shaft seal 1-6-7 and the protective gas shaft seal 1-6-11 are made of polytetrafluoroethylene (PTFE). The lateral length of the idle section of the feeding screw 1-6-2 is 100mm, and the length of the conveying section is 600mm. The inner diameter of the inlet pipe 1-6-10 of the external pressure protective gas structure 1-6-3 is 4mm, and the outer diameter is 6mm. The inlet pipe 1-6-10 is connected to an argon cylinder and a gas quality controller. The outlet pipe 1-6-12 of the external pressure protective gas structure 1-6-3 is connected to an electrically controlled needle valve. The lateral length of the annular cavity of the external pressure protective gas structure 1-6-3 is 4mm. A solid preheater 1-6-13 is installed outside the conveying section of the feeding screw 1-6-2. The outlet of the conveying section merges with the outlet of the first feeding device and is connected to the inlet end of the feeding riser 1-3.

[0146] The feed riser 1-3 is a seamless steel pipe with an outer diameter of 12 mm and a wall thickness of 1.5 mm (inner diameter of 9 mm). The feed riser 1-3 is inserted vertically into the reactor 2-1 along the axis of the reactor 2-1. The outlet of the feed riser 1-3 is located 20 mm from the distribution plate. The height of the experimental static bed is 100 mm.

[0147] The dense phase section (the first cylindrical section with constant diameter) of reactor 2-1 has an inner diameter of 60 mm and a height of 120 mm; the dilute phase section (the third cylindrical section with constant diameter) has an inner diameter of 140 mm and a height of 400 mm; a frustum-shaped transition section (the second cylindrical section with variable diameter) with a sidewall angle of 30° to the axis is used in the middle, and the height of the second cylindrical section is 70 mm; a built-in small cyclone separator 2-3 is used to replace the traditional filter to separate the regenerated flue gas from the bed. The specific structure of the cyclone separator 2-3 is as follows. Figure 3 As shown; a gas distribution plate 2-4 (with a filtration accuracy of 3μm) is installed at the bottom of reactor 2-1, and the gas distribution plate is 20mm away from the bottom of the first section of the cylinder; a regenerant outlet is installed on the side wall of the transition section (the second section of the cylinder with a variable diameter), and the regenerant outlet is connected to an overflow pipe (discharge riser 3-1) with an inner diameter of 9mm. After the discharged particles overflow into the discharge riser 3-1, they enter the regenerated storage bin 3-3 and the particle sampling bottle 3-6 through the particle diversion valve 3-2;

[0148] The flue gas sampling inlet of the flue gas sampling pipe 5-1 (inner diameter 3mm, length 800mm) is located below the bed inside reactor 2-1, and the flue gas sampling outlet is located outside reactor 2-1. The flue gas sampling pipe extends out of reactor 2-1 via the regeneration flue gas outlet at the top of reactor 2-1. The flue gas sampling pipe 5-1 is configured to move axially up and down within reactor 2-1 to sample the regeneration flue gas at different axial positions within the bed inside reactor 2-1. A temperature sensor is also installed at the sampling end of the flue gas sampling pipe 5-1 to obtain the bed temperature. The outlet of the flue gas sampling pipe 5-1 is connected to a three-way valve 5- One opening of valve 3 is connected; of the remaining two openings of the three-way valve 5-3, one is connected to the flue gas sampling bag 5-4, and the other is connected to the sampling flue gas analyzer 5-5; the flue gas inlet of cyclone separator 2-3 is located below the bed of reactor 2-1, the flue gas outlet of cyclone separator 2-3 is located at the top of reactor 2-1, and is connected to the tail gas analyzer 5-6; the reactor back pressure valve 5-7 is set on the connecting pipeline between the flue gas outlet of cyclone separator 2-3 and the tail gas analyzer 5-6, and is used to control the pressure inside reactor 2-1 by adjusting the opening of the reactor back pressure valve 5-7.

[0149] Using the above Figures 1 to 5 The system shown was evaluated for the performance of continuous catalytic cracking flue gas desulfurization and denitrification additives, specifically including the following steps:

[0150] (1) Pretreatment steps: Evaluate the reaction gas required for the reaction by connecting it to a compressed air cylinder, and select a catalytic cracking precursor with a bulk density of 880 kg / m³. 3 The particle density is 1480 kg / m³ 3 The skeleton density is 2650 kg / m³. 3 The carbon content is 1.3% by weight, and the hydrogen-to-carbon molar ratio is 1.3. 8 kg of the pre-treatment agent and 500 g of the target denitrification aid were pre-dried at 200°C for 2 hours.

[0151] (2) Steady-state preparation steps: First, load 302g of the balancing agent with similar properties to the granular agent into the main agent storage silo 1-1. Turn on all instruments, set the gas preheating temperature of gas preheater 4-3 to 200℃, and set the heating temperature of heating furnace 2-2 to 700℃. Start gas intake. The reaction gas (air) required for evaluation passes through pressure regulating valve 4-1, gas flow meter 4-2, and gas preheater 4-3 in sequence. After being heated to 200℃ by gas preheater 4-3, it enters gas pre-distribution chamber 2-5, and then is evenly distributed upwards to the bottom of the reaction chamber of reactor 2-1 by gas distribution plate 2-4. The gas intake flow rate of the reaction gas is 14L / min, and the apparent gas velocity of the reaction gas is 0.12m / s. Adjust the reactor back pressure valve 5-1 at the outlet of cyclone separator 2-3 in reactor 2-1 to make the pressure inside reactor 2-1 0.15MPa. Turn on the first feeding device 1-2 to add the equalizing agent to reactor 2-1. The feeding rate of the first feeding device is 0.84 g / s, and feeding is continued into reactor 2-1 for 6 minutes. After equilibration, the bed balancer content is 252 g (the bed content of reactor 2-1 is 252 g, and the total injected balancer content is 302 g, that is, the total injected balancer content is 1.2 times the bed content of reactor 2-1). Stop air intake and feeding.

[0152] The main agent to be recycled is then loaded into the main agent storage silo 1-1, and the denitrification aid to be evaluated is loaded into the aid storage silo 2-4. The main agent to be recycled enters reactor 2-1 through the first feeding device 1-2 at a feeding rate of 0.84 g / s, and the reaction gas (air) required for evaluation continues to be introduced into reactor 2-1. The reaction gas comes into contact with the main agent, reacts and releases heat, and the heating furnace 2-2 begins to reduce its temperature output, so that the temperature inside reactor 2-1 is kept constant at 700℃. The regenerated agent flows out of reactor 2-1 through the discharge riser 3-1 and enters the regeneration storage silo 3-3. The regeneration flue gas flows out from the cyclone separator 2-3 at the top of reactor 2-1 and is analyzed by the tail gas analyzer 5-4.

[0153] During the steady-state preparation period, the flow rate of the reaction gas and the feeding rate of the main agent are adjusted according to the instrument. Feeding continues, and during the feeding period, multiple CO2 concentration data points in the steady-state preparation regeneration flue gas are acquired within a preset second acquisition and analysis cycle (20 seconds in this embodiment). Then, the second concentration standard deviation σ of the multiple steady-state preparation regeneration flue gas CO2 concentration data points (15 CO2 concentration data points in this embodiment) is used as the basis for the analysis. CO2 'Determine whether the composition of pollutants in the flue gas prepared for regeneration has reached a steady state; when σ CO2 When the concentration is below 0.5%, it indicates that the composition of the regenerated flue gas is stable and the internal temperature of reactor 2-1 remains stable. This means that the balance agent originally laid in reactor 2-1 has been completely replaced, the fluidization and reaction state of the reactor bed are stable, and subsequent steady-state evaluation experiments can begin.

[0154] (3) Evaluation of experimental steps: The regenerated flue gas flows out from the cyclone separator 2-3 at the top of the reactor 2-1 and is analyzed by the tail gas analyzer 5-4. Since no additives are introduced at this time (the additive content is 0% by weight), the data obtained is used as the data of the blank experimental group.

[0155] Then, increase the output speed of the second feeding device to add the denitrification aid into reactor 2-1 at a feeding rate of 0.0093 g / s (9.3 mg / s), that is, the denitrification aid accounts for 1% by weight of the total amount (total amount of regenerator and denitrification aid) (the relationship between the feeding rate and weight ratio will be calibrated before the experiment). After the exhaust gas results stabilize, parameters are collected. The method to determine the stability of the regenerated flue gas composition includes: the regenerated flue gas flows out from the cyclone separator 2-3 at the top of reactor 2-1 and is analyzed by the exhaust gas analyzer 5-4: within the preset first collection and analysis cycle (20 s in this embodiment), multiple CO2 concentration data in the regenerated flue gas are acquired (15 CO2 concentration data in this embodiment); then, based on the first concentration standard deviation σ of the multiple regenerated flue gas CO2 concentration data... CO2 To determine whether the composition of pollutants in the regenerated flue gas has reached a steady state, when σ CO2 When the carbon content is below 0.5%, the composition of the regenerated flue gas reaches a steady state; and by rotating the particle sampling valve 3-5, approximately 1g of regenerator particles are collected in the particle sampling bottle to obtain the carbon content data of the regenerator. Denitrification performance evaluation data are obtained when the denitrification aid accounts for 1% by weight of the total amount (total amount of regenerator and aid).

[0156] Furthermore, during the stable window period, relevant data can be obtained through pressure sensor 5-2 (bed pressure data), three-way valve 5-3, flue gas sampling bag 5-4, sampling flue gas analyzer 5-5 (regenerated flue gas composition data), and temperature sensor 5-8 (bed temperature data). The flue gas sampling tube 5-5 can also be moved from bottom to top to collect parameters at four points in the axial height of the bed (the height difference between adjacent axial test points is 20mm) to obtain the correspondence between flue gas composition and axial height. Figure 6 This is a graph showing the NO concentration versus axial height under these operating conditions. Figure 6It can be seen that under the preset mass ratio condition (1 wt%) of the denitrification aid, the pollutant concentration (NO concentration) in the regenerated flue gas in the reactor bed first increases and then gradually decreases with increasing axial position. The pollutant concentration in the regenerated flue gas is lowest at an axial position of 20 mm from the gas distribution plate, and highest at an axial position of 40 mm from the gas distribution plate. This analysis result can provide data support for research on the generation mechanism and distribution of flue gas pollutants in industrial regeneration processes, the effect and location of denitrification aids, and in-situ treatment of pollutants. For example, this embodiment found that less pollutant is generated at the bottom during the catalyst regeneration process, and the denitrification process occurs more in the middle and upper parts. Therefore, in the development of catalysts for denitrification through regeneration of this type of spent agent, the particle density of the denitrification aid should be made equal to or slightly smaller than that of the spent agent, so that more aid appears in the middle and upper parts, thereby improving the denitrification efficiency.

[0157] Subsequently, the feeding rate of the second feeding device was increased, and experiments and data acquisition were conducted with the denitrification additive accounting for 2%, 3%, 4%, and 5% of the total amount (different preset mass ratios). (The exhaust gas flowed out from cyclone separators 2-3 and was analyzed by exhaust gas analyzer 5-4; the steady-state determination method of exhaust gas composition after changing the mass ratio of the additive was compared with the aforementioned first concentration standard deviation σ.) CO2 The judgment method is the same.

[0158] After the experiment, the data were processed, and the concentrations of pollutants, such as NH3, in the regenerated flue gas after the composition stabilized under different mass ratios of the additives were compared. This was compared with the NH3 concentration in the blank group (the NH3 concentration in the blank experimental group was 142 ppm), and the NH3 removal rate was calculated to evaluate the performance of the denitrification additives. The relationship between the NH3 removal rate in the regenerated flue gas and the mass ratio of the denitrification additives is shown in the graph below. Figure 7 As shown.

[0159] Depend on Figure 7It can be seen that the denitrification effect is related to the mass ratio of the denitrification aid: Firstly, compared with the blank experimental group, the addition of this denitrification aid resulted in a NH3 removal rate of more than 60% in the flue gas, and the higher the proportion of the aid, the less NH3 pollutants in the flue gas; however, as the mass ratio of the denitrification aid increases, the rate of pollutant reduction slows down. Taking the reduction of NH3 in the flue gas as an example, when the mass ratio of the denitrification aid is 1%, 2%, 3%, 4%, and 5% of the total, the NH3 removal rates in this embodiment are 62%, 69%, 75%, 79%, and 80%, respectively; when the denitrification aid is used in an industrial plant to treat the same recycled agent, when the mass ratio of the denitrification aid is 1%, 2%, 3%, 4%, and 5% of the total, the NH3 removal rates are 60%, 68%, 75%, 77%, and 79%, respectively, indicating that the NH3 removal rate in the regenerated flue gas in this embodiment is similar to that of the industrial plant under the same mass ratio conditions.

[0160] Furthermore, in this embodiment, when the mass percentage of the denitrification aid is 1% by weight, the relationship between NO and NH3 in the regenerated flue gas and time is as follows: Figure 8 As shown. By Figure 8 It can be seen that in this embodiment, the concentrations of NO and NH3 pollutants in the flue gas reached a steady state and remained constant after a period of increase, with the NO concentration stabilizing at 165 ppm and the NH3 concentration stabilizing at 57 ppm.

[0161] In addition, the regenerator particles obtained from particle sampling bottles with different proportions of denitrification aids were sent to a carbon-sulfur analyzer and an organic element analyzer to analyze the carbon content of the regenerator. The results showed that the carbon content (C2) of the regenerator was 0.09% by weight for all different proportions of denitrification aids used in this regeneration operation, indicating that the denitrification aid has a relatively small impact on the coking effect of the reactor. When the same regenerator was treated in an industrial plant, the carbon content (C2) of the regenerator was also 0.09% by weight when the denitrification aid accounted for 1%, 2%, 3%, 4%, and 5% of the total mass.

[0162] The above results demonstrate that the performance evaluation effect of the evaluation method provided in this disclosure is close to the actual situation of industrial equipment, and the evaluation results are accurate.

[0163] Example 2

[0164] This implementation is used for performance evaluation of denitrification agents with high denitrification requirements. The same system as in Example 1 is used.

[0165] The difference between this embodiment and Example 1 is that the evaluation of high denitrification requirements has higher requirements for the concentration of nitrogen-containing gases in the reaction gas. The reaction gas introduced in this embodiment is a mixture of NH3, O2 and N2, wherein NH3 is 800 ppm, O2 concentration is 21% by volume, and the remainder is nitrogen. The operation and parameters of the evaluation experiment are the same as those in Example 1, so as to evaluate the denitrification effect in a high NH3 environment.

[0166] Experimental results show that the NH3 concentration in the regenerated flue gas obtained from the blank experimental group (without added denitrification aid) was 786 ppm. With a denitrification aid concentration of 1% by weight, the NH3 concentration in the regenerated flue gas decreased to 173 ppm, and the NH3 removal rate was 78% (between 60% and 90%), indicating that the aid has a good denitrification effect. Other indicators (e.g., the carbon content C2 of the regenerator remained at 0.09% by weight) showed no significant impact. When this denitrification aid was used in an industrial plant to treat the same high-desnitrification-demand regenerator, the NH3 removal rate was 76% under the same denitrification aid concentration conditions. This demonstrates that the performance evaluation effect of the evaluation method provided in this disclosure is close to the actual situation of industrial plants.

[0167] Example 3

[0168] This embodiment is used to evaluate the desulfurization performance of conventional regeneration operations, and uses the same system as in Example 1.

[0169] The difference between this embodiment and Embodiment 1 is that the primary agent to be evaluated is replaced with a desulfurization evaluation primary agent (from a refinery with high sulfur content in the feed oil), and the auxiliary agent is replaced with the desulfurization auxiliary agent to be evaluated. The reaction gas introduced in this embodiment is air. The operation and parameters of the evaluation experiment are the same as in Embodiment 1. Furthermore, the target for flue gas analysis is changed to sulfur-containing compounds, primarily SO2.

[0170] Experimental results show that the SO2 concentration in the regenerated flue gas obtained from the blank experimental group (without added desulfurization additive) was 211 ppm. When the mass ratio of the desulfurization additive was 1% by weight of the total amount of the pre-ferrous metal and the additive, the SO2 removal rate was 83% (between 80% and 95%), indicating that the additive had a good desulfurization effect. When the same pre-ferrous metal was treated in an industrial plant, the SO2 removal rate was 81% when the mass ratio of the desulfurization additive was 1% by weight of the total amount. This indicates that the performance evaluation effect of the evaluation method provided in this disclosure is close to the actual situation of industrial plants.

[0171] Example 4

[0172] This implementation is used for performance evaluation of denitrification agents with high desulfurization requirements, and uses the same system as in Example 3.

[0173] The difference between this embodiment and Example 3 is that the reaction gas is a mixture of SO2, O2 and N2, wherein SO2 is 1500 ppm, O2 concentration is 21% by volume, and the remainder is N2. The evaluation experiment is performed in the same manner as in Example 3.

[0174] Experimental results showed that the SO2 concentration in the regenerated flue gas obtained from the blank experimental group (without adding desulfurization additives) was 1681 ppm;

[0175] When the desulfurization aid accounts for 1% by weight of the total amount of pre-fermented waste and aid, the SO2 removal rate is 92% (between 80% and 95%), indicating that the aid has a good desulfurization effect under a high sulfur oxide atmosphere. When treating the same pre-fermented waste with high desulfurization requirements in an industrial plant, under the same desulfurization aid mass ratio, the SO2 removal rate is 91%. This demonstrates that the performance evaluation effect of the evaluation method provided in this disclosure is close to the actual situation of industrial plants.

[0176] Example 5

[0177] The difference between this embodiment and Embodiment 1 is that:

[0178] The reaction conditions controlled within reactor 2-1 include: a temperature of 450℃, a pressure of 0.6MPa, and an apparent gas velocity of 1m / s.

[0179] The remaining process is the same as in Example 1.

[0180] In this embodiment, the NO concentration in the stabilized regenerated flue gas is 12 ppm, and the NH3 concentration is 0 ppm; the carbon content of the regenerator is 1% by weight. When the same regenerator is treated in an industrial plant, the NO concentration is 160 ppm, the NH3 concentration is 55 ppm, and the carbon content of the regenerator is 0.09% by weight, all at the same mass percentage.

[0181] It can be seen that the degree of reaction varies under different reaction conditions during the evaluation experiment in reactor 2-1. Specifically, the NO and NH3 concentrations and carbon content of the regenerated flue gas in this embodiment differ significantly from those of the industrial plant's regenerated flue gas composition and regenerated agent carbon content. Furthermore, comparing this embodiment with Example 1, when Example 1 was evaluated using the system provided in this disclosure, the reaction conditions in reactor 2-1 met the following criteria: temperature 650–750℃; pressure 0.15–0.25 MPa; apparent gas velocity of the reaction gas 0.1–0.6 m / s. The regenerated flue gas composition and regenerated agent carbon content obtained from the evaluation experiment in Example 1 are closer to those of the industrial plant, meaning the reaction process is closer and the evaluation results are more accurate.

[0182] Comparative Example 1

[0183] The difference between Comparative Example 1 and Example 1 is that:

[0184] The same denitrification aid as in Example 1 was evaluated using a fixed fluidized bed reactor. Before the experiment, the same pretreated denitrification aid and the main agent were weighed and mixed at 0 wt%, 1 wt%, 2 wt%, 3 wt%, 4 wt%, and 5 wt%, and then placed into the fixed fluidized bed for reaction.

[0185] The changes in NO and NH3 concentrations in flue gas over time when the additive percentage is 1% by weight are as follows: Figure 9 As shown, when the fixed fluidized bed evaluation device uses a mixture of pre-regenerating agent and denitrification aid to simulate the actual regeneration environment, it cannot replicate its continuous and stable state. Without the replenishment of the pre-regenerating agent, the amount of nitrogen-containing compounds on the pre-weighed pre-regenerating agent decreases, and it cannot reach a steady state.

[0186] Furthermore, this comparative example... Figure 9 Compared with Example 1 Figure 8 The comparison shows that Example 1 can reach a steady state as the reaction time progresses, while in this comparative example, the concentrations of NO and NH3 begin to decrease after reaching their maximum values ​​of 130 ppm and 32 ppm respectively, until the signal disappears.

[0187] Furthermore, when using a fixed fluidized bed reactor for evaluation, each concentration ratio experiment requires separate material loading. Therefore, the apparatus must be cooled down after each experiment, material loaded, and then heated up again. This is extremely time-consuming, and this waste becomes more pronounced as the number of experiments increases. It is also difficult to ensure that, apart from the set control variables, other variables remain consistent across different conditions in the same group of experiments over such a long time span.

[0188] Comparative Example 2

[0189] The difference between Comparative Example 2 and Example 1 is that:

[0190] Using a filter instead of cyclone separator 2-3: As the evaluation time progresses, the filter pores become clogged by fluidized bed sedimentation and entrainment into the dilute phase space, causing changes in the overall pressure drop of the filter. For an experiment requiring stable operation with low target compound concentration and high experimental precision, this leads to reduced reliability and repeatability of the evaluation work. In contrast, this disclosure uses cyclone separator 2-3 to separate the regenerated flue gas from reactor 2-1, maintaining the steady state of reactor 2-1 and ensuring the reliability and repeatability of the evaluation work.

[0191] Comparative Example 3

[0192] The difference between Comparative Example 3 and Example 1 is that:

[0193] Using the same flooding and valve-controlled material discharge method as industrial reactors, under otherwise unchanged conditions, problems arise with the discharge rate at the bottom of reactor 2-1 when switching between different feed rates, gas flow rates, and gas pressures. For example, a larger pressure differential will increase the discharge rate and lower the bed density, requiring precise control of the valve opening. Simultaneously, valve wear will negatively impact the control effectiveness. This disclosure employs an overflow discharge method, which helps maintain a stable bed density.

[0194] Comparative Example 4

[0195] The difference between Comparative Example 4 and Example 1 is that:

[0196] This comparative example uses only one feeding device connected to feed riser 1-3. During the reaction, a pre-mixed denitrification aid and a pre-treated agent at a predetermined mass ratio are added to the storage silo of the feeding device. After conducting an experiment with a denitrification aid mass ratio of 1 wt%, the device is shut down and allowed to cool down. Simultaneously, the reactor, feeder, and storage silo are cleaned to prevent residual material from affecting the actual concentration in the next set of experiments. Then, a denitrification aid and pre-treated agent mixture at a mass ratio of 2 wt% is mixed in the tank, and the experiment is restarted. Experiments with other denitrification aid proportions also require repeated batching, preheating, steady-state preparation, experimentation, shutdown and cooling, and cleaning of the reactor, feeder, and storage silo each time, increasing the reaction time.

[0197] The preferred embodiments of this disclosure have been described in detail above with reference to the accompanying drawings. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0198] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0199] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A method for evaluating the performance of continuous catalytic cracking flue gas desulfurization and denitrification aids, characterized in that, The method includes the following steps: The main agent to be generated is fed into the reactor (2-1) of the regeneration simulation reaction unit through a continuous first feeding device and the desulfurization and denitrification auxiliary agent is fed into the reactor through a continuous second feeding device, respectively, and they are in contact with the reaction gas to carry out a regeneration reaction to obtain regenerated flue gas and regenerator; By adjusting the first feeding speed of the first feeding device for conveying the main agent to be generated and / or adjusting the second feeding speed of the second feeding device for conveying the desulfurization and denitrification aid, the mass ratio of the main agent to the desulfurization and denitrification aid entering the reactor (2-1) can be controlled to be a number of different preset mass ratios; When the mass ratio of the main agent to the desulfurization and denitrification aid is adjusted to each preset mass ratio, the composition of the regenerated flue gas obtained by the regeneration reaction in reactor (2-1) under the preset mass ratio condition is obtained. Furthermore, in the process of obtaining the composition of regenerated flue gas under each preset mass ratio condition, the method further includes: when the composition of pollutants in the regenerated flue gas under the preset mass ratio condition reaches a steady state, the composition of the regenerated flue gas after the steady state is taken as the composition of the regenerated flue gas under the preset mass ratio condition. Based on the pollutant concentrations in the regenerated flue gas composition obtained under each preset mass ratio condition, the performance of the desulfurization and denitrification aids in the regeneration reaction under that preset mass ratio condition is evaluated.

2. The method according to claim 1, characterized in that, The method also includes: The lower the concentration of pollutants in the regenerated flue gas, the better the performance of the desulfurization and denitrification aid under the given mass ratio conditions.

3. The method according to claim 1, characterized in that, In the process of obtaining the composition of regenerated flue gas under each preset mass ratio condition, the method further includes: Within a preset first data acquisition and analysis period, multiple CO2 concentration data in the regenerated flue gas under the preset mass ratio conditions are acquired; then, based on the first concentration standard deviation σ of the acquired multiple CO2 concentration data... CO2 Determine whether the composition of pollutants in the regenerated flue gas under the preset mass ratio condition has reached a steady state.

4. The method according to claim 3, characterized in that, The preset first data acquisition and analysis cycle time is 1~20s.

5. The method according to claim 4, characterized in that, The preset first data acquisition and analysis cycle time is 1~5s.

6. The method according to claim 3, characterized in that, The method also includes: when the first concentration standard deviation σ CO2 When the pollutant content is below 0.5%, the composition of pollutants in the regenerated flue gas reaches a steady state under this preset mass ratio condition.

7. The method according to claim 6, characterized in that, The method also includes: when the first concentration standard deviation σ CO2 When the content is below 0.2%, the composition of pollutants in the regenerated flue gas reaches a steady state under the preset mass ratio condition.

8. The method according to claim 6, characterized in that, The first concentration standard deviation σ CO2 The number of CO2 concentration data points required for the calculation is 10 to 60.

9. The method according to claim 8, characterized in that, The first concentration standard deviation σ CO2 The number of CO2 concentration data points required for the calculation is 20 to 40.

10. The method according to claim 1, characterized in that, The method also includes: The main agent to be generated is fed into the reactor (2-1) via a continuous first feeding device and comes into contact with the reaction gas to carry out a regeneration reaction, resulting in blank group regenerated flue gas and blank group regenerator; the blank group regenerated flue gas is collected and analyzed to obtain the composition of the blank group flue gas. The performance of the desulfurization and denitrification aid under the preset mass ratio condition is evaluated based on the difference in pollutant concentration between the regenerated flue gas obtained by the regeneration reaction of the desulfurization and denitrification aid introduced at the preset mass ratio and the regenerated flue gas of the blank group.

11. The method according to claim 10, characterized in that, The method also includes: The greater the difference in pollutant concentration between the regenerated flue gas and the blank group regenerated flue gas, the better the performance of the desulfurization and denitrification aid under the preset mass ratio condition.

12. The method according to claim 1, characterized in that, Prior to step S1, the method also includes a step of preparing for a steady-state experiment.

13. The method according to claim 12, characterized in that, The steady-state experiment preparation steps include: A balancing agent is pre-set in the reactor (2-1), and then the main agent to be generated is fed into the reactor (2-1) through the continuous first feeding device, and regenerated by contacting the reaction gas to obtain steady-state ready-to-regenerate flue gas and steady-state ready-to-regenerate agent; and the balancing agent is discharged through the outlet of the reactor (2-1) to replace the balancing agent; The steady-state preparation regeneration flue gas is led out through the flue gas outlet of reactor (2-1), and the steady-state preparation regenerator is discharged through the discharge port of reactor (2-1); Within the preset second data acquisition and analysis period, multiple steady-state CO2 concentration data in the prepared regeneration flue gas are acquired; then, based on the second concentration standard deviation σ of the multiple steady-state prepared regeneration flue gas CO2 concentration data... CO2 'Determine whether the composition of pollutants in the flue gas prepared for regeneration has reached a steady state.' 14. The method according to claim 13, characterized in that, The preset second data acquisition and analysis cycle time is 1~20s.

15. The method according to claim 14, characterized in that, The preset second acquisition and analysis cycle time is 1~5s.

16. The method according to claim 13, characterized in that, The second concentration standard deviation σ CO2 The number of CO2 concentration data points required for the calculation is 10 to 60.

17. The method according to claim 16, characterized in that, The second concentration standard deviation σ CO2 The number of CO2 concentration data points required for the calculation is 20 to 40.

18. The method according to claim 13, characterized in that, The method also includes: When the second concentration standard deviation σ CO2 The content of pollutants in the regenerated flue gas is below 0.5%, and the composition of pollutants in the steady-state preparation flue gas reaches a steady state.

19. The method according to claim 18, characterized in that, The method also includes: When the second concentration standard deviation σ CO2 The content of pollutants in the regenerated flue gas is below 0.2%, indicating that the composition of pollutants in the regenerated flue gas has reached a steady state.

20. The method according to claim 1, characterized in that, The feeding unit includes the first feeding device, the second feeding device, and the feed riser (1-3); the method further includes: The main agent to be produced is fed to the feed riser (1-3) by the first feeding device and then enters the reactor (2-1); the desulfurization and denitrification aid is fed to the feed riser (1-3) by the second feeding device and then enters the reactor (2-1).

21. The method according to claim 20, characterized in that, The reactor (2-1) has a regenerant outlet on its side wall, and a discharge riser (3-1) is connected to the outside of the regenerant outlet; the method further includes: Solid particles in the reactor (2-1) overflow into the discharge riser (3-1) through the regenerant outlet on the side wall of the reactor (2-1); and then flow out of the reactor (2-1) through the discharge riser (3-1) into the regenerant recovery and analysis unit.

22. The method according to claim 21, characterized in that, The solid particles include regenerators and desulfurization and denitrification aids.

23. The method according to claim 21, characterized in that, The method includes: causing the solid particles in the reactor (2-1) to flow out through the discharge riser (3-1) and then be divided into two parts by the particle diversion valve (3-2); causing one part of the solid particles to enter the regeneration storage bin (3-3) and the other part of the solid particles to enter the particle sampling bottle (3-6).

24. The method according to claim 1, characterized in that, The reactor (2-1) is axially provided with a flue gas sampling pipe (5-1) penetrating the top of the reactor (2-1), and the flue gas sampling pipe (5-1) is movable along the axial direction of the reactor (2-1); the opening of the flue gas sampling pipe (5-1) inside the reactor (2-1) forms a flue gas sampling inlet, and the opening of the flue gas sampling pipe (5-1) outside the reactor (2-1) forms a flue gas sampling outlet, the flue gas sampling outlet being used to connect to a flue gas composition detection device; the method further includes: Move the flue gas sampling tube (5-1) up and down along the axial direction of the reactor (2-1) to collect regenerated flue gas samples obtained from different axial positions of the bed in the reactor (2-1); The regenerated flue gas samples collected at each location are processed as follows: the regenerated flue gas samples flow out of the reactor (2-1) through the flue gas sampling outlet of the flue gas sampling tube (5-1) and are divided into two regenerated flue gas samples; one regenerated flue gas sample enters the flue gas sampling bag (5-4), and the other regenerated flue gas sample enters the sampling flue gas analyzer (5-5) to obtain the composition of the regenerated flue gas at that location.

25. The method according to claim 24, characterized in that, The axial height difference between two adjacent positions in different axial positions is 1~500mm; the axial movement speed of the flue gas sampling tube (5-1) from top to bottom or from bottom to top is 0.5~5mm / s.

26. The method according to claim 24, characterized in that, The method also includes selecting 3 to 50 regenerated flue gas samples with different axial positions.

27. The method according to claim 24, characterized in that, The method further includes: obtaining the pressure at each bed location by passing a regenerated flue gas sample at a pressure sensor (5-2); and then evaluating the stability of the bed pressure at different axial positions in the reactor (2-1) based on the pressure of the regenerated flue gas samples at different axial positions.

28. The method according to claim 1, characterized in that, The reactor (2-1) is provided with a gas distribution plate (2-4) at its lower part, and the reactor (2-1) is divided into a gas pre-distribution chamber (2-5) and a reaction chamber by the gas distribution plate (2-4), with the gas distribution plate (2-4) as the boundary, and the gas pre-distribution chamber (2-5) is located below the reaction chamber; the method further includes: The reaction gas is sequentially introduced into the gas pre-distribution chamber (2-5) of the reactor (2-1) via a pressure regulating valve (4-1), a gas flow meter (4-2), and a gas preheater (4-3). Then, the gas enters the reaction chamber of the reactor (2-1) through the gas distribution plate (2-4) and comes into contact with the solid particles in the reactor (2-1); wherein the solid particles include the main agent and the desulfurization and denitrification aid.

29. The method according to claim 28, characterized in that, The method also includes: The reaction gas is preheated to 10~300°C by a gas preheater (4-3) and then enters the gas pre-distribution chamber (2-5).

30. The method according to claim 29, characterized in that, The method also includes: The reaction gas is preheated to 100~250°C by a gas preheater (4-3) and then enters the gas pre-distribution chamber (2-5).

31. The method according to claim 1, characterized in that, When evaluating denitrification performance: The main component has a carbon content of 0.5-3% by weight, a carbon-hydrogen molar ratio of 0.2-3, and a bulk density of 700-1000 kg / m³. 3 The particle density is 1200~1600 kg / m³ 3 The skeletal density is 2300~2800 kg / m³. 3 ; When evaluating desulfurization performance: the carbon content of the main desulfurizing agent should be 0.5-3% by weight, the carbon-hydrogen molar ratio should be 0.2-3, and the bulk density should be 700-1000 kg / m³. 3 The particle density is 1200~1600 kg / m³ 3 The skeletal density is 2300~2800 kg / m³. 3 ; The reaction gas is selected from one or more of air, oxygen, nitric oxide, ammonia, carbon monoxide, and nitrogen.

32. The method according to claim 31, characterized in that, When evaluating the denitrification performance: the NO concentration in the regenerated flue gas obtained from the regeneration reaction is 0~1000ppm, the NO2 concentration is 0~1000ppm, the HCN concentration is 0~1000ppm, and the NH3 concentration is 0~1000ppm; When evaluating desulfurization performance: the SO₂ content in the regenerated flue gas obtained from the regeneration reaction... X Concentration range: 0~3000ppm; The volume content of oxygen in the reaction gas is 0 to 100% by volume.

33. The method according to claim 32, characterized in that, The oxygen content in the reaction gas is 21-40% by volume.

34. The method according to claim 1, characterized in that, The feeding rate of the desulfurization and denitrification aid is 0.001~20 g / s; the feeding rate of the pre-fermentation main agent is 0.1~20 g / s; the mass ratio of the desulfurization and denitrification aid to the pre-fermentation main agent in reactor (2-1) is 0.01~1:1; The reaction conditions inside reactor (2-1) include: temperature of 500~800℃; pressure of 0~0.5MPa; The apparent gas velocity of the reactant gas is 0.01~0.8 m / s.

35. The method according to claim 34, characterized in that, The mass ratio of desulfurization and denitrification aid to pre-fermentation agent in reactor (2-1) is 0.01~0.1:1; The reaction conditions in reactor (2-1) include: temperature of 650~750℃; pressure of 0.15~0.25MPa; and apparent gas velocity of the reaction gas of 0.1~0.6m / s.

36. A performance evaluation system for continuous catalytic cracking flue gas desulfurization and denitrification additives, characterized in that, The system includes: a feeding unit, a regeneration simulation reaction unit, a gas supply unit, a regeneration flue gas acquisition and analysis unit, and a regenerator recovery and analysis unit; The feeding unit includes a continuous first feeding device and a continuous second feeding device; the first feeding device includes a discharge port for the main agent to be produced, and the second feeding device includes a discharge port for the desulfurization and denitrification auxiliary agent; The regeneration simulation reaction unit includes a reactor (2-1), which includes a feed inlet, a reaction gas inlet, a regeneration flue gas outlet, and a regenerator outlet. The feed inlet is connected to the main agent outlet of the first feeding device and the desulfurization and denitrification auxiliary agent outlet of the second feeding device, respectively. The regeneration flue gas outlet is connected to the regeneration flue gas acquisition and analysis unit. The regenerator outlet is connected to the regenerator recovery and analysis unit. The first and second feeding devices include feeding structures with identical structures; the feeding structure includes: a storage bin, a feeding screw (1-6-2), and an external pressure protection gas structure (1-6-3); the feeding screw (1-6-2) includes an idle section, a feeding section, and a transmission section; The external pressure protective gas structure (1-6-3) includes an external pressure protective gas housing (1-6-4), a clamping end cap (1-6-5), and a pellet feeder housing (1-6-6). The external pressure protective gas housing (1-6-4) is sleeved outside the empty section of the feeding screw (1-6-2), and the clamping end cap (1-6-5) is located at the end of the empty section. The clamping end cap (1-6-5) and the first end face of the external pressure protective gas housing (1-6-4) are sealed by a protective gas shaft seal (1-6-11). The inner wall of the external pressure protective gas housing (1-6-4) and the outer wall of the feeding screw (1-6-2) have a gap to form an annular cavity around the feeding screw (1-6-2). The external pressure protective gas housing (1-6-4) is provided with an inlet pipe (1-6-10) and an outlet pipe (1-6-12) that connect the inside and outside, so that the annular cavity is connected to the gas source through the inlet pipe (1-6-10) and connected to the outside of the external pressure protective gas housing (1-6-4) through the outlet pipe (1-6-12).

37. The system according to claim 36, characterized in that, The transverse length of the annular cavity is 0.5~8mm.

38. The system according to claim 37, characterized in that, The intake pipe (1-6-10) is equipped with a pressure sensor and a control valve; the exhaust pipe (1-6-12) is equipped with a back pressure valve. The pellet feeder housing (1-6-6) is sleeved outside the feeding section of the feeding screw (1-6-2), and the first end face of the pellet feeder housing (1-6-6) and the second end face of the external pressure protective gas housing (1-6-4) are sealed by a feeding shaft seal (1-6-7). The feed screw outlet of the first feeding device is formed as the discharge port of the main agent to be produced; the feed screw outlet of the second feeding device is formed as the discharge port of the desulfurization and denitrification auxiliary agent.

39. The system according to claim 38, characterized in that, The regeneration simulation reaction unit also includes a feed riser (1-3); the inlet of the feed riser (1-3) is located outside the reactor (2-1), and the outlet of the feed riser (1-3) is located inside the reactor (2-1); the inlet of the feed riser (1-3) is connected to the outlet of the main agent to be generated and the outlet of the desulfurization and denitrification auxiliary agent of the feeding unit respectively.

40. The system according to claim 39, characterized in that, The regenerated flue gas acquisition and analysis unit includes a flue gas sampling tube (5-1), a pressure sensor (5-2), a three-way valve (5-3), a flue gas sampling bag (5-4), and a sampling flue gas analyzer (5-5). The flue gas sampling pipe (5-1) is installed through the regenerated flue gas outlet at the top of the reactor (2-1); the opening of the flue gas sampling pipe (5-1) inside the reactor (2-1) forms a flue gas sampling inlet, and the opening of the flue gas sampling pipe (5-1) outside the reactor (2-1) forms a flue gas sampling outlet; and the flue gas sampling pipe (5-1) is configured to move axially up and down within the reactor (2-1) to sample the regenerated flue gas at different axial positions of the bed within the reactor (2-1); The outlet of the flue gas sampling tube (5-1) is connected to one opening of the three-way valve (5-3); of the remaining two openings of the three-way valve (5-3), one is connected to the flue gas sampling bag (5-4), and the other is connected to the sampling flue gas analyzer (5-5).

41. The system according to claim 40, characterized in that, A gas sealing structure is provided at the position where the flue gas sampling pipe (5-1) connects to the regenerated flue gas outlet of the reactor (2-1).

42. The system according to claim 40, characterized in that, The pressure sensor (5-2) is installed on the connecting pipeline between the outlet of the flue gas sampling pipe (5-1) and the three-way valve (5-3).

43. The system according to claim 40, characterized in that, The regenerated flue gas acquisition and analysis unit also includes a cyclone separator (2-3), a tail gas analyzer (5-6), and a reactor back pressure valve (5-7). The flue gas inlet of the cyclone separator (2-3) is located below the bed of the reactor (2-1), and the flue gas outlet of the cyclone separator (2-3) is located at the top of the reactor (2-1) and is connected to the tail gas analyzer (5-6). The reactor back pressure valve (5-7) is installed on the connecting pipeline between the flue gas outlet of the cyclone separator (2-3) and the tail gas analyzer (5-6) to control the pressure inside the reactor (2-1) by adjusting the opening of the reactor back pressure valve (5-7).

44. The system according to claim 36, characterized in that, The reactor (2-1) is provided with a gas distribution plate (2-4) at the bottom, and the reactor (2-1) is divided into an upper gas pre-distribution chamber (2-5) and a lower reaction chamber by the gas distribution plate (2-4); the reaction gas inlet is located at the bottom of the gas pre-distribution chamber (2-5); The gas supply unit includes a pressure regulating valve (4-1), a gas flow meter (4-2), and a gas preheater (4-3) connected in sequence; the preheated reaction gas outlet of the gas preheater (4-3) is connected to the reaction gas inlet of the gas pre-distribution chamber (2-5); The regenerant recovery and analysis unit includes a discharge riser (3-1), a particle diversion valve (3-2), a regenerated storage bin (3-3), a discharge valve (3-4), a particle sampling valve (3-5), and a particle sampling bottle (3-6). The discharge riser (3-1) is located outside the reactor (2-1), and the regenerant outlet of the reactor (2-1) is connected to the upper inlet of the discharge riser (3-1) so that the regenerant in the reactor (2-1) overflows into the discharge riser (3-1); the lower outlet of the discharge riser (3-1) is connected to the inlet of the particle diversion valve (3-2); the particle diversion valve (3-2) includes a first diversion outlet and a second diversion outlet; the first diversion outlet is connected to the particle sampling bottle (3-6) via the particle sampling valve (3-5); the second diversion outlet is connected to the inlet of the regenerated storage silo (3-3); the discharge valve (3-4) is located on the outlet pipeline at the bottom of the regenerated storage silo (3-3).

45. The system according to claim 44, characterized in that, One or more heating devices are also provided outside the reactor (2-1).

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