A method and device for separating and recovering methanol-to-aromatics catalyst fines by cyclone coupling radial micro-channel

Abstract

The application discloses a methanol-to-aromatics catalyst fine powder cyclone coupling radial micro-channel separation and recovery method and device, relates to the field of purification treatment technology, and comprises the following steps: product gas generated by a methanol-to-aromatics reactor and regenerated flue gas generated by a methanol-to-aromatics regenerator are respectively introduced into a first multi-stage cyclone separation assembly and a second multi-stage cyclone separation assembly, the product gas in the first multi-stage cyclone separation assembly and the regenerated flue gas in the second multi-stage cyclone separation assembly are subjected to preliminary separation of catalyst large-diameter particles and gas by centrifugal action; through multi-element physical action mechanisms such as direct interception, inertial collision and gravity deposition of a micro-channel, efficient interception of catalyst fine powder is realized; a device matched with the device integrates a cyclone separator, a radial micro-channel separator, a catalyst storage tank, a quench tower and a water washing tower, each unit cooperatively operates, separation efficiency is high, energy consumption is low, and there is no secondary pollution.

Description

Technical Field

[0001] This application relates to the field of purification and treatment technology, specifically to a method and apparatus for separating and recovering methanol-to-aromatics catalyst micropowder using cyclone coupling radial microchannels. Background Technology

[0002] Methanol-to-aromatics (MTO) is a key technology in the integrated development of modern coal chemical and petrochemical industries. It utilizes acidic catalysts to directionally convert methanol feedstock into high-value-added aromatics such as benzene, toluene, and xylene. The economics and product quality of the process largely depend on the activity stability and loss control of the catalyst. In actual operation, the catalytic conversion process in the reactor and the catalyst recycling in the regenerator are both conducted in harsh environments of high temperature and high-speed gas-solid flow. Under the combined effects of continuous high-temperature gas flow, interparticle collision abrasion, and chemical reaction erosion, the ZSM-5 molecular sieve catalyst gradually breaks down and refines, generating a large amount of fine powder with a particle size distribution of 0.1–50 μm. These catalyst microparticles escape from the system with the product gas and regeneration flue gas, not only causing the loss of effective catalyst components (accounting for approximately 30% to 40% of the total loss and significantly increasing feedstock consumption costs), but also potentially causing pipe blockage, equipment wear, reduced heat transfer efficiency, and even exacerbating equipment corrosion by carrying acidic components. Therefore, the generation and dispersion of catalyst microparticles has become a key issue affecting the long-term stable operation of the plant, restricting the economic competitiveness of the process, and hindering its green development.

[0003] The efficient separation and recovery of catalyst microparticles has become a core issue in the optimization of methanol-to-aromatics processes. Existing technologies mainly rely on single separation devices or simple coupled systems, but all have significant shortcomings. Traditional cyclone separators are widely used due to their large capacity and low cost, but their centrifugal force field significantly reduces their ability to capture microparticles smaller than 20 μm, with separation efficiency typically below 80%, making it difficult to meet the requirements for high-precision recovery. While membrane filtration technology can retain submicron particles, it is prone to membrane pore blockage in the high-temperature and high-dust environments of methanol-to-aromatics processes, requiring frequent shutdowns for cleaning, leading to decreased system stability and significantly increased energy consumption. Electrostatic separation technology enhances microparticle removal through charge adsorption, but it is significantly affected by factors such as gas humidity and dust resistivity, exhibiting poor adaptability in the complex operating conditions of methanol-to-aromatics regeneration flue gas. Axial microchannel separation equipment, while having high separation efficiency, is limited by its structural design, with a single unit capacity typically <5000 Nm³ / h, making it difficult to match the large-scale gas production demands of methanol-to-aromatics units and limiting its large-scale application.

[0004] Chinese patent application CN101384685B discloses a method for removing fine catalyst particles from a reaction system, applicable to molecular sieve catalytic reaction systems such as methanol-to-olefins. This technology addresses the problem of fine catalyst particles entrained in the reaction product gas and regenerator flue gas by incorporating multi-stage separation units within the system to remove catalyst particles from the gas, thereby reducing catalyst loss caused by its emission with the gas and minimizing the impact of fine particles on subsequent equipment and the environment. This patent primarily focuses on the removal and emission control of fine catalyst particles.

[0005] Chinese patent application CN1942558B discloses a method for wet washing and recovering catalyst particles in an olefin production process using oxygen-containing compounds. This technology introduces gas carrying catalyst particles during the reaction or regeneration process into the washing system, allowing the catalyst particles to enter the liquid phase and be recycled, thereby reducing catalyst loss. While this method achieves catalyst particle recovery to some extent, it relies on wet washing, which can easily lead to catalyst powder entering the water system, increasing the burden on wastewater treatment.

[0006] Chinese patent application CN109134182A discloses a separation system and process for separating product gas and catalyst in a methanol-to-olefins (MTO) reaction. This technology addresses the problem of fine catalyst powder entrained in the product gas during the methanol conversion reaction by incorporating a further catalyst removal unit on top of a multi-stage cyclone separator. This reduces the proportion of fine powder entering the quench tower and scrubbing system, thereby mitigating wear and clogging risks in downstream equipment. While this solution improves the purification effect of the product gas, its separation method still primarily relies on filtration or trapping structures, limiting its stability during continuous operation under high-temperature and high-dust conditions.

[0007] Chinese patent application CN101353187B discloses a method and apparatus for purifying reaction wastewater in a methanol-to-olefins process. This technology addresses the problem of fine catalyst particles entering the wastewater system during quenching and washing processes by employing methods such as cyclone separation to separate the catalyst particles entrained in the wastewater, thereby reducing the solids content and lessening the load on subsequent treatment. While this patent addresses the treatment of fine catalyst powder from the perspective of the water system, it does not solve the problem of efficient separation of catalyst microparticles in the gas phase.

[0008] In summary, existing methanol-to-aromatics and similar methanol-to-methanol conversion molecular sieve catalytic reaction systems primarily rely on multi-stage cyclone separation, filtration, or wet scrubbing techniques for the separation and recovery of catalyst powder. While these technologies can reduce catalyst loss or meet emission requirements to some extent, they generally suffer from the following shortcomings: First, traditional cyclone separation has limited efficiency for separating catalyst powder with small particle sizes; second, filtration or wet scrubbing methods are prone to clogging, scaling, or increased system pressure drop under high-temperature, high-dust, and continuous operation conditions; third, existing technologies mainly focus on removal or emission control, lacking a technical solution that can achieve efficient and stable separation of fine catalyst powder in the gas phase and facilitate its recycling. Therefore, there is an urgent need for a catalyst powder separation and recovery method and device suitable for methanol-to-aromatics reactions and regeneration systems, to achieve efficient retention and resource recovery of catalyst powder while ensuring large throughput and continuous operational stability. Summary of the Invention

[0009] The purpose of this application is to provide a method and apparatus for separating and recovering methanol-to-aromatics catalyst micropowder via cyclone coupling radial microchannel in order to solve the above-mentioned problems and overcome the defects of the prior art.

[0010] To achieve the above objectives, this application provides the following technical solutions:

[0011] In a first aspect, embodiments of this application provide a method for the separation and recovery of methanol-to-aromatics catalyst micropowder via cyclone coupling radial microchannels, comprising the following steps:

[0012] S1: The product gas generated by the methanol-to-aromatics reactor and the regenerated flue gas generated by the methanol-to-aromatics regenerator enter the first multi-stage cyclone separation component and the second multi-stage cyclone separation component, respectively. The product gas in the first multi-stage cyclone separation component and the regenerated flue gas in the second multi-stage cyclone separation component both utilize centrifugal force to achieve preliminary separation of large-diameter catalyst particles from the gas.

[0013] S2: The separated product gas and regenerated gas are respectively fed into the first radial microchannel separator and the second radial microchannel separator. With the help of the direct interception, inertial collision, gravity deposition and diffusion deposition mechanisms in the microchannel, the residual catalyst powder in the gas is further removed.

[0014] S3: Backflush nitrogen is used to periodically purge the catalyst powder trapped in the first and second radial microchannel separators, causing the powder to detach from the microchannels and be transported to the first and second catalyst tanks respectively, ensuring the continuous and efficient operation of the microchannel separators;

[0015] S4: The product gas separated by the first radial microchannel separator is then subjected to a two-stage water washing system for deep purification before being transported to the olefin separation system. At the same time, the regenerated flue gas after the above treatment is directly transported to the boiler unit.

[0016] In some embodiments of the first aspect, in step S1, both the first multi-stage cyclone separation component and the second multi-stage cyclone separation component are composed of a three-stage cyclone separator and a four-stage cyclone separator. The linear velocity of the gas entering the three-stage cyclone separator is 18 to 22 m / s, the initial concentration of the catalyst is 500 to 2000 mg / Nm³, and the concentration of large-particle catalyst after separation is ≤400 mg / Nm³.

[0017] In some embodiments of the first aspect, in step S1, the linear velocity of the gas entering the four-stage cyclone separator is 20 to 25 m / s, the initial concentration of the catalyst is 100 to 400 mg / Nm³, and the concentration of large-particle catalyst after separation is ≤200 mg / Nm³.

[0018] In some embodiments of the first aspect, in step S2, the operating temperature of the first radial microchannel separator for processing the product gas is 80 to 120°C, the gas flow rate is 0.8 to 1.5 m / s, and the catalyst concentration after separation is ≤10 mg / Nm³.

[0019] In some embodiments of the first aspect, in step S2, the operating temperature of the second radial microchannel separator for processing the regenerated flue gas is 120 to 150°C, the gas flow rate is 1.0 to 2.0 m / s, and the catalyst concentration after separation is ≤15 mg / Nm³.

[0020] In some embodiments of the first aspect, the pressure of the backflushing nitrogen gas in step S3 is 0.2 to 0.8 MPa, the purging frequency is once every 0.5 to 2 hours, the particle size of the purged catalyst powder is ≤20 μm, and it is transported to the first catalyst storage tank and the second catalyst storage tank respectively through pneumatic conveying pipelines.

[0021] Secondly, this application also provides a methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device, including a methanol-to-aromatics reactor and a methanol-to-aromatics regenerator connected to each other, a first multi-stage cyclone separation component connected to the methanol-to-aromatics reactor, and a second multi-stage cyclone separation component connected to the methanol-to-aromatics regenerator, for the preliminary separation of large-diameter particles of the catalyst.

[0022] The first radial microchannel separator is connected to the first multi-stage cyclone separation assembly, and the second radial microchannel separator is connected to the second multi-stage cyclone separation assembly for further separation of catalyst micropowder;

[0023] A two-stage water washing system is set between the first radial microchannel separator and the olefin separation system in the product gas path for cooling and purifying the product gas. The two-stage water washing system includes a quench tower and a water washing tower connected in series.

[0024] The first catalyst storage tank is connected to the first radial microchannel separator via a nitrogen backflushing pipeline, and the second catalyst storage tank is connected to the second radial microchannel separator via a nitrogen backflushing pipeline, for receiving and storing catalyst powder purged by backflushing nitrogen, respectively.

[0025] In some embodiments of the second aspect, the first radial microchannel separator triggers backflushing nitrogen once every 1 to 2 hours, and the second radial microchannel separator triggers backflushing once every 0.5 to 1 hour, to ensure effective purging and recovery of catalyst powder.

[0026] Both the first and second radial microchannel separators are made of corrosion-resistant, high-strength metal alloys or ceramic materials, and the radial microchannel pressure drop of both the first and second radial microchannel separators does not exceed 10 kPa.

[0027] In some embodiments of the second aspect, the cylinder diameter D1 of the three-stage cyclone separator is 800 to 1200 mm, the guide vanes adopt a logarithmic helix angle of 15 to 20°, and the discharge port diameter is ≤D1 / 3.

[0028] In some embodiments of the second aspect, the cylinder diameter D2 of the four-stage cyclone separator is 600 to 1000 mm, the guide vanes adopt a logarithmic helix angle of 20 to 25°, and the discharge port diameter is ≤D2 / 2.5.

[0029] The embodiments of this application have the following advantages:

[0030] 1. Through multiple physical mechanisms such as direct interception of microchannels, inertial collision, and gravity deposition, the catalyst powder is efficiently retained. The supporting device integrates a cyclone separator, a radial microchannel separator, a catalyst storage tank, a quench tower, and a water washing tower. All units work together to achieve high separation efficiency, low energy consumption, and no secondary pollution.

[0031] 2. By adopting a coupling technology of cyclone separation and radial microchannel separation, large-diameter particles are initially removed by centrifugal force, and then micro-powder is deeply retained by the multi-element physical action within the microchannel, forming a hierarchical separation system. This breaks through the limitation of single technology in handling particles with a wide particle size range, and achieves efficient separation of catalysts across the entire particle size range.

[0032] 3. The design incorporates a periodic backflushing mechanism, which can promptly remove microparticles trapped in the microchannels, avoiding the clogging problems common in traditional separation technologies, reducing the frequency of system downtime maintenance, ensuring continuous and stable operation, and adapting to the long-term production needs of the methanol-to-aromatics process.

[0033] 4. The device features a compact integrated design. The radial microchannel separator is made of heat-resistant and corrosion-resistant materials, which can adapt to the complex working conditions of high temperature and high dust in the methanol-to-aromatics process. It can also be easily connected to existing production systems and can be applied without large-scale modifications, thus providing feasibility for industrial promotion. Attached Figure Description

[0034] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0035] Figure 1 This is a flow chart of the methanol-to-aromatics catalyst micropowder cyclone coupling radial microchannel separation and recovery process of this application;

[0036] Figure 2 This is a schematic diagram of the structure of the first radial microchannel separator of this application;

[0037] Figure 3 This is a schematic diagram of the structure of the second radial microchannel separator of this application.

[0038] The reference numerals in the attached drawings are explained as follows: 1. Methanol-to-aromatics reactor; 101. Reactor cyclone separation unit; 2. First multi-stage cyclone separation assembly; 3. First radial microchannel separator; 301. First exhaust port; 302. First catalyst powder outlet; 303. First air inlet; 304. First backflushing nitrogen interface; 305. First axial guide pipe; 306. First filling zone; 4. Quenching tower; 5. Water washing tower; 6. First catalyst storage tank; 7. Methanol-to-aromatics regenerator; 701. Regenerator cyclone separation unit; 8. Second multi-stage cyclone separation assembly; 9. Second radial microchannel separator; 901. Second exhaust port; 902. Second catalyst powder outlet; 903. Second air inlet; 904. Second backflushing nitrogen interface; 905. Second axial guide pipe; 906. Second filling zone; 10. Second catalyst storage tank. Detailed Implementation

[0039] To make the objectives, technical solutions, and advantages of this application clearer, the technical solutions of this application will be described in detail below. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. Based on the embodiments in this application, all other implementation methods obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0040] After extensive and in-depth research, the inventors of this application discovered that in the methanol-to-aromatics process, the catalyst is eroded by high-temperature airflow, particle collision, and chemical reaction, forming micropowder that is discharged with the product gas and regeneration flue gas. This results in catalyst loss, increased costs, equipment blockage, reduced efficiency, and environmental pollution, hindering the green and efficient development of the process. In existing technologies, traditional cyclone separators are inefficient at separating micropowder smaller than 20μm, membrane filtration technology is prone to blockage and has high energy consumption in high-temperature and high-dust environments, electrostatic separation is greatly affected by flue gas humidity, and axial microchannel equipment has limited processing capacity, making it difficult to balance large processing volume with high-precision retention, leading to high catalyst loss, high costs, and environmental pollution from micropowder emissions. Therefore, this invention presents a cyclone-coupled radial microchannel separation and recovery method for methanol-to-aromatics catalyst micropowder. The accompanying device integrates a cyclone separator, a radial microchannel separator, a catalyst storage tank, a quench tower, and a water washing tower. These units operate collaboratively to solve the aforementioned technical problems, featuring high separation efficiency, low energy consumption, and no secondary pollution.

[0041] See Figures 1 to 3 As shown, this application provides a method for the separation and recovery of methanol-to-aromatics catalyst micropowder using cyclone coupling radial microchannels, comprising the following steps:

[0042] S1. The product gas generated by the methanol-to-aromatics reactor 1 and the regenerated flue gas generated by the methanol-to-aromatics regenerator 7 enter the first multi-stage cyclone separator 2 and the second multi-stage cyclone separator 8, respectively. Both the product gas in the first multi-stage cyclone separator 2 and the regenerated flue gas in the second multi-stage cyclone separator 8 utilize centrifugal force to achieve preliminary separation of large-diameter catalyst particles from the gas; see the appendix to the instruction manual. Figure 1 As shown, the methanol-to-aromatics reactor 1 is equipped with a reactor cyclone separation unit 101 for pre-separation, and the methanol-to-aromatics regenerator 7 is equipped with a regenerator cyclone separation unit 701 for pre-separation. Both the reactor cyclone separation unit 101 and the regenerator cyclone separation unit 701 are composed of a primary cyclone separator and a secondary cyclone separator connected in series.

[0043] In some embodiments, in step S1, within the methanol-to-aromatics reactor 1, both the first multi-stage cyclone separation component 2 and the second multi-stage cyclone separation component 8 consist of a three-stage cyclone separator and a four-stage cyclone separator. The linear velocity of the gas entering the three-stage cyclone separator is 18 to 22 m / s, the initial catalyst concentration is 500 to 2000 mg / Nm³, and the concentration of large catalyst particles after separation is ≤400 mg / Nm³. Through the above structural design, the separation principle of the cyclone separator relies on the centrifugal force generated by the gas rotation to throw the catalyst particles against the cylinder wall to achieve separation. When the linear velocity of a three-stage cyclone separator is below 18 m / s, the centrifugal force is insufficient, reducing its ability to retain medium-sized particles (20-50 μm), and the concentration after separation easily exceeds 400 mg / Nm³. If the linear velocity exceeds 22 m / s, although the centrifugal force will further increase, the flow resistance of the gas inside the cylinder will increase sharply. Since resistance is proportional to the square of the velocity, this leads to increased system pressure drop and increased fan energy consumption. Simultaneously, the particles carried by the high-speed airflow will exacerbate erosion and wear on the internal structure of the separator, shortening the equipment's service life. A linear velocity range of 18-22 m / s achieves the optimal balance between high-efficiency separation and low energy consumption and low wear.

[0044] See instruction manual attached Figure 1 As shown, the first multi-stage cyclone separator 2 has two outlets connected to the first radial microchannel separator 3 via pipes. These two outlets are respectively located on the third-stage and fourth-stage cyclone separators. Similarly, the second multi-stage cyclone separator 8 has two outlets connected to the second radial microchannel separator 9 via pipes. These two outlets are also located on the third-stage and fourth-stage cyclone separators. This design is a bypass design. In actual industrial processes, bypass pipes are used to handle unexpected situations (such as equipment failure, abnormal system pressure, etc.) or to perform specific debugging operations. Under certain conditions, gas can be directly discharged through the bypass pipe without passing through the complete four-stage cyclone separator filtration process. For example, when the third-stage cyclone separator detects a blockage or other fault, gas can be directly discharged through the bypass pipe to prevent excessive system pressure, ensuring system safety.

[0045] Different operating conditions: Depending on different production conditions or product quality requirements, sometimes a four-stage cyclone separator filtration can meet current production needs. For example, in specific production stages with relatively low product quality requirements, or when the catalyst powder content is already low, it is possible to bypass the four-stage cyclone separator and directly discharge the gas for subsequent processing to improve production efficiency and reduce energy consumption.

[0046] In some embodiments, in step S1, the inlet linear velocity of the gas entering the four-stage cyclone separator is 20 to 25 m / s, the initial catalyst concentration is 100 to 400 mg / Nm³, and the concentration of large catalyst particles after separation is ≤200 mg / Nm³. The pre-processing equipment for the four-stage cyclone separator is a three-stage cyclone separator. After three-stage separation, the remaining catalyst particles in the gas are mainly small to medium-sized particles with a diameter of 10-20 μm. The centrifugal force required for these particles is higher than that for large-diameter particles. The linear velocity range of 20-25 m / s for the four-stage cyclone separator can efficiently capture small particles while balancing energy consumption and equipment durability.

[0047] S2. The separated product gas and regenerated gas are respectively fed into the first radial microchannel separator 3 and the second radial microchannel separator 9. By means of the direct interception, inertial collision, gravity deposition and diffusion deposition mechanisms in the microchannel, the residual catalyst powder in the gas is further removed.

[0048] The four mechanisms of action mentioned above—direct interception, inertial collision, gravity deposition, and diffusion deposition—are not independent but rather work synergistically based on the particle size differences of the residual catalyst powder after multi-stage cyclone separation, covering the removal needs of powders in different particle size ranges.

[0049] Direct interception: For micro powders of 5-10μm, when gas flows through the microchannel, the particles are directly intercepted on the channel surface because their particle size is larger than the gap between the microchannels or their movement trajectory comes into contact with the channel wall.

[0050] Inertial collision: For 2-5μm micro powders, when the gas flows through bends or narrow slits in the microchannel, the micro powder cannot follow the airflow in time due to inertia and is trapped after colliding with the channel wall.

[0051] Gravity deposition: For micro powders of 1-2μm, the particles slowly settle to the bottom of the channel under the influence of gravity during the relatively long residence time in the microchannel, thus completing the separation.

[0052] Diffusion deposition: For submicron-sized powders ≤1μm, random diffusion occurs due to Brownian motion, eventually contacting the channel wall and being adsorbed and retained, filling the gap in the ability of traditional cyclone separation to remove submicron-sized powders.

[0053] For the product gas to subsequently enter the two-stage water washing system consisting of quench tower 4 and water washing tower 5, the low-concentration micro powder after microchannel separation can reduce the blockage of the trays in quench tower 4, reduce the solid content of quench wastewater, and reduce wastewater treatment costs; for the regenerated flue gas to enter the subsequent boiler, the low-concentration micro powder can reduce the catalyst residue in the boiler ash and reduce the difficulty of ash and ash treatment.

[0054] In some embodiments, in step S2, the operating temperature of the first radial microchannel separator 3 for processing the product gas is 80 to 120°C, the gas flow rate is 0.8 to 1.5 m / s, and the catalyst concentration after separation is ≤10 mg / Nm³. The first radial microchannel separator 3 relies on physical mechanisms such as direct interception and inertial collision to remove fine powder. When the temperature is above 120°C, the excessively high temperature will cause the thermal motion of gas molecules to intensify, and the Brownian motion of submicron-sized microparticles will be enhanced, making them easier to escape through diffusion deposition. When the temperature is below 80°C, the gas viscosity will increase, and the flow resistance of the airflow in the microchannel will increase, resulting in a weakening of the inertial collision effect. The temperature range of 80-120°C can ensure that the separation mechanisms such as direct interception, inertial collision, gravity deposition, and diffusion deposition work synergistically.

[0055] In some embodiments, in step S2, the operating temperature of the second radial microchannel separator 9 for processing the regenerated flue gas is 120 to 150°C, the gas flow rate is 1.0 to 2.0 m / s, and the catalyst concentration after separation is ≤15 mg / Nm³.

[0056] S3. Backflushing nitrogen is used to periodically purge the catalyst powder trapped in the first radial microchannel separator 3 and the second radial microchannel separator 9, causing the powder to detach from the microchannels and be transported to the catalyst tank, ensuring the continuous and efficient operation of the first radial microchannel separator 3 and the second radial microchannel separator 9. Without backflushing, the radial microchannel separators usually become clogged after 8-12 hours of operation, with the pressure drop rising to over 15 kPa, requiring shutdown, disassembly, and cleaning. After periodic backflushing nitrogen purging, combined with the "72-hour long-term operational stability" data, the pressure drop of the first and second radial microchannel separators stabilizes at 5-9 kPa, with no clogging, and the continuous operating time of the equipment is greatly improved.

[0057] In some embodiments, in step S3, the pressure of the backflushing nitrogen gas is 0.2 to 0.8 MPa, the purging frequency is once every 0.5 to 2 hours, the particle size of the purged catalyst powder is ≤20 μm, and it is transported to the first catalyst storage tank 6 and the second catalyst storage tank 10 through pneumatic conveying pipelines respectively.

[0058] S4. The product gas separated by the first radial microchannel separator 3 is then subjected to a two-stage water washing system for deep purification before being transported to the olefin separation system. At the same time, the regenerated flue gas after the above treatment is directly transported to the boiler unit.

[0059] The technical concept of this application is as follows:

[0060] See instruction manual attached Figure 1As shown, the reaction in the methanol-to-aromatics reactor 1 causes the catalyst to gradually deactivate. The deactivated catalyst and other materials need to be transported through pipelines to the methanol-to-aromatics regenerator 7 for regeneration. Conversely, after regenerating the catalyst in the methanol-to-aromatics regenerator 7, the regenerated catalyst and other materials are returned to the methanol-to-aromatics reactor 1 through pipelines. This ensures the continuous and efficient operation of the methanol-to-aromatics reaction, forming a cyclical process of catalyst reaction, deactivation, regeneration, and re-reaction. The product gas generated in the methanol-to-aromatics reactor 1 and the regenerated flue gas generated in the methanol-to-aromatics regenerator 7 enter the first multi-stage cyclone separator 2 and the second multi-stage cyclone separator 8, respectively. Centrifugal force is used to achieve preliminary separation of large-diameter catalyst particles from the gas. The inlet linear velocity of the three-stage cyclone separator is 18-22 m / s, and the concentration of large-particle catalyst after separation is ≤400 mg / L. The inlet linear velocity of the four-stage cyclone separator is 20-25 m / s, and the concentration of large catalyst particles after separation is ≤200 mg / Nm³. The product gas and regenerated flue gas after preliminary separation are then passed into the first radial microchannel separator 3 and the second radial microchannel separator 9, respectively. With the help of direct interception, inertial collision, gravity deposition and diffusion deposition in the microchannel, residual catalyst powder is further removed. The powder retained by the two radial microchannel separators is periodically purged every 0.5-2 hours to remove the powder with a particle size ≤20 μm from the channel and transport it to the corresponding catalyst storage tank. The product gas separated by the first radial microchannel separator 3 is then deeply purified by a two-stage water washing system consisting of a quench tower 4 and a water washing tower 5 connected in series, and then transported to the olefin separation system. The regenerated flue gas treated by the second radial microchannel separator 9 is directly transported to the boiler unit.

[0061] A methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device includes: a methanol-to-aromatics reactor 1 and a methanol-to-aromatics regenerator 7 connected to each other; a first multi-stage cyclone separation component 2 connected to the methanol-to-aromatics reactor 1; and a second multi-stage cyclone separation component 8 connected to the methanol-to-aromatics regenerator 7, for the preliminary separation of large-diameter particles of the catalyst.

[0062] The first air inlet 303 of the first radial microchannel separator 3 is connected to the first multi-stage cyclone separator 2. The first radial microchannel separator 3 is also provided with a first backflushing nitrogen port 304 for introducing backflushing nitrogen. The first radial microchannel separator 3 is provided with a first catalyst powder outlet 302, which is connected to the first catalyst storage tank 6 through a pipe. The first radial microchannel separator 3 is provided with a first exhaust port 301, which is connected to the two-stage water washing system.

[0063] The second air inlet 903 of the second radial microchannel separator 9 is connected to the second multi-stage cyclone separator 8. The second radial microchannel separator 9 is also provided with a second backflushing nitrogen port 904 for introducing backflushing nitrogen. The second radial microchannel separator 9 is provided with a second catalyst powder outlet 902, which is connected to the second catalyst storage tank 10 through a pipe. The second radial microchannel separator 9 is provided with a second exhaust port 901, which is connected to the boiler device.

[0064] The quench tower 4 and the water washing tower 5 are connected in sequence to the first radial microchannel separator 3 on the product gas path for cooling and purifying the product gas;

[0065] The first catalyst storage tank 6 is connected to the first radial microchannel separator 3 via a nitrogen backflushing pipeline, and the second catalyst storage tank 10 is connected to the second radial microchannel separator 9 via a nitrogen backflushing pipeline, for receiving and storing catalyst powder purged by backflushing nitrogen gas respectively.

[0066] The first radial microchannel separator 3 is triggered to backflush once every 1 to 2 hours, and the second radial microchannel separator 9 is triggered to backflush once every 0.5 to 1 hour, to ensure effective purging and recovery of catalyst powder.

[0067] The first radial microchannel separator 3 and the second radial microchannel separator 9 are both made of corrosion-resistant, high-strength metal alloys or ceramic materials, and the radial microchannel pressure drop of the first radial microchannel separator 3 and the second radial microchannel separator 9 does not exceed 10 kPa.

[0068] See instruction manual attached Figure 2 and Figure 3 As shown, the radial microchannel separator adopts a vertical cylindrical structure, and its main structural parameters are set as follows:

[0069] The inner diameter of the housing of the two radial microchannel separators is 1200-2200 mm, and the total height of the separators is 3500-6500 mm; the inner diameter of the axial guide tube located in the center of the housing is 150-350 mm, and the length is 1200-2500 mm.

[0070] As shown in the figure, the lower end of the axial guide tube is connected to a conical diverter. The cone angle of the conical diverter is 35-55° and the cone height is 300-800mm. It is used to uniformly convert the axial airflow into radially distributed airflow.

[0071] A radial microchannel separation region is formed on the outer periphery of the axial guide tube. This radial microchannel separation region is composed of an internal filling area and a continuous lateral space formed between the filling area and the inner wall of the shell. Its parameters are set as follows:

[0072] The outer diameter of the filling area is 70% to 85% of the inner diameter of the shell;

[0073] The effective height of the filling area is 1500–3500 mm;

[0074] The lateral space between the filling area and the inner wall of the shell is 40–150 mm wide.

[0075] Lateral space is used to form a low-velocity buffer zone, which significantly reduces the gas velocity after it enters the separation zone radially. Under typical operating conditions with a gas throughput of 30,000 Nm³ / h, the apparent gas velocity entering the separation zone radially is controlled within the range of 0.8–2.0 m / s.

[0076] Under the above structural parameters and operating conditions, catalyst microparticles with different particle sizes exhibit distinct separation behavior in the radial microchannel separator:

[0077] Catalyst micropowder with a particle size ≥5μm deviates from the gas streamline due to inertia in the early stage of radial entry into the separation zone and is directly intercepted by contact with the filling zone or the surface of the separator structure.

[0078] Catalyst micropowder with a particle size of 2–5 μm undergoes inertial collisions and is captured under the influence of changes in gas flow direction and local velocity gradients;

[0079] Catalyst micropowder with a particle size of 1-2 μm gradually migrates downward and settles under the conditions of reduced flow rate and extended residence time in the separation zone, thus achieving gravity deposition;

[0080] Submicron-sized catalyst powder with a particle size ≤1μm is affected by Brownian diffusion in the lateral space and near the surface of the filling area, and achieves diffusion deposition through multiple surface contacts.

[0081] Under the aforementioned industrial conditions, after radial microchannel separation, the concentration of catalyst powder in the gas decreased from 300–1200 mg / Nm³ to 8–15 mg / Nm³, and the overall separation efficiency reached 90%–97%.

[0082] The cylinder diameter D1 of the three-stage cyclone separator is 800 to 1200 mm, the guide vanes adopt a logarithmic helix angle of 15 to 20°, and the discharge port diameter is ≤D1 / 3. The cylinder diameter D2 of the four-stage cyclone separator is 600 to 1000 mm, the guide vanes adopt a logarithmic helix angle of 20 to 25°, and the discharge port diameter is ≤D2 / 2.5.

[0083] This application addresses catalyst microparticles carried in the reactor product gas and regenerator flue gas of a methanol-to-aromatics (DMTA) unit, which belongs to a high-temperature, high-velocity gas-solid system. Due to the change from a liquid to a gas phase in the continuous phase, the movement mechanism of catalyst particles in the separator shifts from being dominated by sedimentation to being dominated by inertial collisions and direct interception, with diffusion deposition playing a supplementary role for submicron particles. Under these conditions, the sedimentation and low-velocity displacement mechanisms relied upon in liquid-phase microchannels are physically untenable; therefore, this application cannot be simply considered a transfer of wastewater microchannel technology.

[0084] The radial microchannel separator in this application is not a general microchannel structure, but a radial arrangement specifically designed for gas-solid systems. This arrangement causes a change in gas direction within the channel, causing catalyst powder to deviate from the gas streamline due to inertia and collide with the channel walls, thus being trapped. This structure forms a hierarchical progression with multi-stage cyclone separation: the cyclone separator mainly removes larger catalyst particles, while the radial microchannel separator is specifically designed for fine catalyst powders smaller than 20 micrometers, where cyclone separation efficiency significantly decreases, thus solving the physical limitations of multi-stage cyclones within this particle size range.

[0085] Meanwhile, this application considers backflushing operation as a necessary technical condition for the continuous operation of the radial microchannel separator under gas phase conditions, rather than merely a conventional anti-clogging measure. Through backflushing, the catalyst powder deposited on the microchannel wall can be promptly detached and enter the recovery system, forming a closed-loop system of "cyclone pre-separation - radial microchannel deep separation - backflushing recovery".

[0086] (I) Performance test results of cyclone separator (Table 1)

[0087] Experimental conditions:

[0088] This experiment focuses on the cyclone separators in a methanol-to-aromatics (DMTA) unit, testing their separation performance in the third-stage cyclone separator handling the product gas and the fourth-stage cyclone separator handling the regenerated flue gas. The product gas was taken from the outlet of the methanol-to-aromatics reactor, and the regenerated flue gas from the outlet of the catalyst regenerator. The experiment was conducted under atmospheric pressure, with the system pressure controlled between 0.095 and 0.105 MPa. The operating temperature of the product gas cyclone separator was 180–220 °C, and the operating temperature of the regenerated flue gas cyclone separator was 350–450 °C. The catalyst used was a molecular sieve catalyst (ZSM-5 system), with an entrained micro-particle size distribution ranging from 0.1 to 50 μm.

[0089] Experimental procedure:

[0090] After the device operated continuously and reached a stable operating condition, the inlet linear velocity of the cyclone separators was adjusted by regulating the gas flow rate. Specifically, the inlet linear velocity of the third-stage cyclone separator was controlled at 18 m / s, 20 m / s, and 22 m / s; the inlet linear velocity of the fourth-stage cyclone separator was controlled at 20 m / s, 22 m / s, and 25 m / s. Under each operating condition, the system was allowed to run stably for at least 30 minutes before sampling tests were conducted to avoid the influence of transient fluctuations on the experimental results. Multiple parallel experiments were performed under each operating condition, and the average value of the results was taken as the test data for that corresponding operating condition.

[0091] Sampling point setup and sampling method:

[0092] Cyclone separation performance testing employed a fixed-point isokinetic sampling method. The inlet sampling point was located in the straight section of the cyclone separator inlet, at least 5 times the pipe diameter from the cyclone inlet, to ensure thorough mixing of the gas and solid phases. The outlet sampling point was located in the gas pipeline at the cyclone separator outlet, at least 3 times the pipe diameter from the cyclone outlet, to minimize the influence of the rotating flow on the sampling results. During sampling, the sampling rate was strictly controlled to match the mainstream velocity within the pipeline, ensuring that the collected samples accurately reflected the actual concentration and particle size distribution of the catalyst particles in the gas.

[0093] Analytical methods and testing instruments:

[0094] The concentration of catalyst powder in the gas was determined by gravimetric method. The sampled gas was passed through a high-temperature resistant filter membrane (0.3 μm pore size) to retain solid particles. The mass of the filter membrane before and after sampling was measured under constant temperature and humidity conditions, and the mass concentration of the catalyst powder was calculated based on the sampled gas volume. Solid samples collected at the inlet and outlet were subjected to particle size distribution testing using a laser particle size analyzer to obtain the separation efficiency within different particle size ranges. The main instruments used in the experiment included a high-temperature isokinetic sampling device, a laser particle size analyzer (measuring range 0.1–100 μm), a high-precision electronic balance (accuracy 0.1 mg), and online temperature and pressure monitoring instruments.

[0095]

[0096] (II) Experimental Description of Separation Performance of Radial Microchannel Separator (corresponding to Table 2)

[0097] Experimental conditions:

[0098] This experiment used a radial microchannel separator as the research object, and tested the separation performance of the first radial microchannel separator for processing methanol-to-aromatics product gas and the second radial microchannel separator for processing regenerated flue gas. The product gas was taken from the downstream end of a multi-stage cyclone separator, and the regenerated flue gas was taken from the downstream end of the regenerator cyclone separation system. The experiment was conducted under atmospheric pressure, with the system pressure controlled between 0.095 and 0.105 MPa. When processing the product gas, the operating temperature of the radial microchannel separator was controlled between 80 and 120 °C, and the gas flow rate between 0.8 and 1.5 m / s; when processing the regenerated flue gas, the operating temperature was controlled between 120 and 150 °C, and the gas flow rate between 1.0 and 2.0 m / s. The catalyst powder entering the radial microchannel separator mainly consisted of fine particles after cyclone separation, with a particle size distribution primarily between 0.1 and 20 μm.

[0099] Experimental procedure:

[0100] Under stable operating conditions of the methanol-to-aromatics unit, the product gas or regenerated flue gas after cyclone separation is introduced into the corresponding radial microchannel separator. The operating temperature and gas flow rate of the separator are stabilized at set values ​​by adjusting the heat exchange and gas flow control systems. Sampling and testing are initiated after the system has been running continuously and stably for at least 30 minutes under each experimental condition to avoid the influence of operating condition fluctuations on the test results. Multiple sets of experiments are conducted for different combinations of temperature and gas flow rates. Multiple parallel tests are performed for each condition, and the average value is taken as the separation performance data under that condition.

[0101] Sampling point setup and sampling method:

[0102] The radial microchannel separation performance was tested using a fixed-point isokinetic sampling method. The inlet sampling point was located on a straight section of the radial microchannel separator's inlet pipe, at least 5 times the pipe diameter from the separator inlet; the outlet sampling point was located on a straight section of the separator's outlet pipe, at least 3 times the pipe diameter from the separator outlet. During sampling, the sampling rate was strictly controlled to match the mainstream gas velocity within the pipe to ensure that the collected samples accurately reflected the actual concentration changes of the catalyst powder in the gas before and after the radial microchannel separator.

[0103] Analytical methods and testing instruments:

[0104] The concentration of catalyst fines in the gas before and after the radial microchannel separator was measured by the gravimetric method. The sampled gas was intercepted by a high-temperature resistant filter membrane for solid particles, and the filter membrane was weighed under constant temperature and humidity conditions, and the mass concentration of catalyst fines was calculated in combination with the volume of the sampled gas. The particle size distribution of the solid samples collected at the inlet and outlet under different operating conditions was tested by a laser particle size analyzer to analyze the separation efficiency of the radial microchannel separator for catalyst fines with different particle sizes. The main instruments used in the experiment included a high-temperature isokinetic sampling device, a laser particle size analyzer (measurement range 0.1 - 100 μm), a high-precision electronic balance (accuracy 0.1 mg), and on-line monitoring instruments for temperature and pressure.

[0105]

[0106] (III) Operation of the backflush nitrogen system and experimental description of catalyst recovery (corresponding to Table 3)

[0107] Experimental conditions:

[0108] In this experiment, the backflush nitrogen system supporting the radial microchannel separator was taken as the research object, and the effects of backflush pressure and purge frequency on the recovery effect of catalyst fines were tested. The experiment was carried out under the condition of continuous and stable operation of the methanol-to-aromatics unit, and the treatment object was the catalyst fines intercepted in the radial microchannel separator. The backflush gas was industrial-grade nitrogen, and the backflush pressures were set at 0.2 MPa, 0.5 MPa, and 0.8 MPa respectively, and the purge frequency was uniformly controlled to be purged once every 1 h. During the experiment, the operating pressure of the system was atmospheric pressure, and the temperature of the separator main body was kept consistent with the product gas or regenerated flue gas temperature under the corresponding operating conditions.

[0109] Experimental procedure:

[0110] After the radial microchannel separator was continuously operated and reached a stable pressure drop state, periodic backflush operations were performed on the separator according to the predetermined backflush parameters. During each backflush process, nitrogen entered the microchannel structure reversely from the backflush interface, so that the catalyst fines intercepted on the microchannel surface were detached from the channel wall under the action of the instantaneous high-pressure gas flow and were carried out. After the backflush, the system immediately resumed the normal separation operation state, and the operating conditions of the separator before and after the backflush were recorded. Multiple backflush experiments were carried out for different backflush pressure conditions, and the catalyst fines recovered each time were collected and statistically analyzed.

[0111] Sampling point setting and sampling method:

[0112] The catalyst microparticles recovered from backflushing are collected centrally through a catalyst discharge port connected to the bottom of a radial microchannel separator. The collection container is weighed before and after each backflushing operation to obtain the catalyst recovery amount corresponding to a single backflushing operation. The recovered catalyst microparticle samples are stored under sealed conditions for subsequent particle size analysis to evaluate the impact of backflushing parameters on the particle size distribution of the recovered catalyst.

[0113] Analytical methods and testing instruments:

[0114] The mass of the catalyst micropowder recovered in a single run was weighed using a high-precision electronic balance, and the recovery amount under different backflushing pressure conditions was calculated. The particle size distribution of the recovered micropowder was tested using a laser particle size analyzer to obtain the average particle size characteristic value. The main testing instruments used in the experiment included a high-precision electronic balance (accuracy 0.1 mg), a laser particle size analyzer (measuring range 0.1–100 μm), and an online monitoring instrument for backflushing nitrogen pressure and flow rate.

[0115]

[0116] (iv) Description of the 72-hour long-term operational stability test (corresponding to Table 4)

[0117] Experimental conditions:

[0118] This experiment was conducted under continuous operation conditions of a methanol-to-aromatics (DMTA) unit to evaluate the long-term operational stability of the cyclone separator-radial microchannel separator-backflushing recovery system. During the experiment, the product gas and regenerated flue gas processed by the system came from the reactor outlet and regenerator outlet under normal production conditions, respectively, and the overall operating pressure of the unit was maintained within the atmospheric pressure range. The operating temperature, gas flow rate, and backflushing nitrogen parameters of the radial microchannel separator were all kept within the optimized operating conditions verified in the aforementioned experiments, without any manual adjustments, to simulate the continuous and stable operation of an industrial unit.

[0119] Experimental procedure:

[0120] After the operating parameters of each unit of the system stabilized, a continuous operation stability test was initiated, and the system ran continuously for 72 hours without shutdown or structural adjustments. Key operating indicators of the system were recorded at 0h, 24h, 48h, and 72h of operation, including the catalyst powder concentration at the product gas outlet, the catalyst powder concentration at the regenerated flue gas outlet, the overall system pressure drop, and the purity of the recovered catalyst. During the experiment, only normal backflushing operations were performed at predetermined intervals, while other operating conditions remained unchanged to examine the performance changes of the system during long-term operation.

[0121] Sampling point setup and sampling method:

[0122] Sampling points for both product gas and regenerated flue gas were set at the straight sections of the outlet pipes of the corresponding radial microchannel separators. Fixed-point isokinetic sampling was used to ensure that the collected samples accurately reflected the actual concentration of catalyst powder in the system outlet gas. Catalyst samples were periodically taken from the catalyst recovery tank to determine changes in its purity. System pressure drop was monitored and recorded in real time by online differential pressure gauges located at both the front and rear ends of the system.

[0123] Analytical methods and testing instruments:

[0124] The concentration of catalyst powder in the product gas and regenerated flue gas was determined by gravimetric method, and the system pressure drop was directly read by an online differential pressure transmitter. The purity of the recovered catalyst was obtained by sieving and analyzing the impurity content of the recovered samples. The main instruments used in the experiment included a high-temperature isokinetic sampling device, a high-precision electronic balance, an online differential pressure monitoring instrument, and conventional physicochemical testing equipment for catalyst purity analysis.

[0125]

[0126] The overall system separation efficiency is ≥94.5%, and the unit energy consumption is ≤2.1kWh / 1000Nm³, which verifies the advantages of high efficiency and low energy consumption.

[0127] During 72 hours of operation, the changes in outlet concentration, pressure drop, and catalyst purity were all ≤5.4%, demonstrating good system stability and no significant performance degradation.

[0128] The above description is merely a specific embodiment of this application, but the scope of protection of this application is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in this application should be included within the scope of protection of this application. Therefore, the scope of protection of this application should be determined by the scope of the claims.

Claims

1. A method for separating and recovering methanol-to-aromatics catalyst micropowder using cyclone coupling radial microchannels, characterized in that: Includes the following steps: S1: The product gas generated by the methanol-to-aromatics reactor and the regenerated flue gas generated by the methanol-to-aromatics regenerator enter the first multi-stage cyclone separation component and the second multi-stage cyclone separation component, respectively. The product gas in the first multi-stage cyclone separation component and the regenerated flue gas in the second multi-stage cyclone separation component both utilize centrifugal force to achieve preliminary separation of large-diameter catalyst particles from the gas. S2: The separated product gas and regenerated gas are respectively fed into the first radial microchannel separator and the second radial microchannel separator. With the help of the direct interception, inertial collision, gravity deposition and diffusion deposition mechanisms in the microchannel, the residual catalyst powder in the gas is further removed. S3: Backflush nitrogen is used to periodically purge the catalyst powder trapped in the first and second radial microchannel separators, causing the powder to detach from the microchannels and be transported to the first and second catalyst tanks respectively, ensuring the continuous and efficient operation of the microchannel separators; S4: The product gas separated by the first radial microchannel separator is then subjected to a two-stage water washing system for deep purification before being transported to the olefin separation system. At the same time, the regenerated flue gas after the above treatment is directly transported to the boiler unit. In step S1, both the first multi-stage cyclone separation component and the second multi-stage cyclone separation component are composed of a three-stage cyclone separator and a four-stage cyclone separator. The linear velocity of the gas entering the three-stage cyclone separator is 18 to 22 m / s, the initial concentration of the catalyst is 500 to 2000 mg / Nm³, and the concentration of large-particle catalyst after separation is ≤400 mg / Nm³. In step S1, the linear velocity of the gas entering the four-stage cyclone separator is 20 to 25 m / s, the initial concentration of the catalyst is 100 to 400 mg / Nm³, and the concentration of large-particle catalyst after separation is ≤200 mg / Nm³. In step S2, the operating temperature of the first radial microchannel separator for processing the product gas is 80 to 120°C, the gas flow rate is 0.8 to 1.5 m / s, and the catalyst concentration after separation is ≤10 mg / Nm³. In step S2, the operating temperature of the second radial microchannel separator for treating the regenerated flue gas is 120 to 150°C, the gas flow rate is 1.0 to 2.0 m / s, and the catalyst concentration after separation is ≤15 mg / Nm³. The pressure of the backflushing nitrogen gas in step S3 is 0.2 to 0.8 MPa, the purging frequency is once every 0.5 to 2 hours, the particle size of the catalyst powder after purging is ≤20 μm, and it is transported to the first catalyst storage tank and the second catalyst storage tank respectively through pneumatic conveying pipelines.

2. A methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device, employing the methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery method described in claim 1, characterized in that: It includes a methanol-to-aromatics reactor and a methanol-to-aromatics regenerator connected to each other. A first multi-stage cyclone separator is connected to the methanol-to-aromatics reactor, and a second multi-stage cyclone separator is connected to the methanol-to-aromatics regenerator for the preliminary separation of large-diameter catalyst particles. The first radial microchannel separator is connected to the first multi-stage cyclone separation assembly, and the second radial microchannel separator is connected to the second multi-stage cyclone separation assembly for further separation of catalyst micropowder; A two-stage water washing system is set between the first radial microchannel separator and the olefin separation system in the product gas path for cooling and purifying the product gas. The two-stage water washing system includes a quench tower and a water washing tower connected in series. The first catalyst storage tank is connected to the first radial microchannel separator via a nitrogen backflushing pipeline, and the second catalyst storage tank is connected to the second radial microchannel separator via a nitrogen backflushing pipeline, for receiving and storing catalyst powder purged by backflushing nitrogen, respectively.

3. The methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device according to claim 2, characterized in that: The first radial microchannel separator triggers backflushing nitrogen once every 1 to 2 hours, and the second radial microchannel separator triggers backflushing once every 0.5 to 1 hour, to achieve the purging and recovery of catalyst powder. Both the first and second radial microchannel separators are made of corrosion-resistant, high-strength metal alloys or ceramic materials, and the radial microchannel pressure drop of both the first and second radial microchannel separators does not exceed 10 kPa.

4. The methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device according to claim 2, characterized in that: The cylinder diameter D1 of the three-stage cyclone separator is 800 to 1200 mm, the guide vanes adopt a logarithmic helix angle of 15 to 20°, and the discharge port diameter is ≤ D1 / 3.

5. The methanol-to-aromatics catalyst micropowder cyclone-coupled radial microchannel separation and recovery device according to claim 2, characterized in that: The cylinder diameter D2 of the four-stage cyclone separator is 600 to 1000 mm, the guide vanes adopt a logarithmic helix angle of 20 to 25°, and the discharge port diameter is ≤D2 / 2.5.

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