Anti-blocking methanol synthesis reactor

Abstract

The invention relates to the technical field of methanol production equipment, in particular to an anti-blocking methanol synthesis reactor which comprises a shell, a central pipe and a catalyst bed layer, a reaction cavity is formed in the shell, and a synthesis gas outlet communicated with the reaction cavity is formed in the shell; the central tube is arranged in the reaction cavity, the end part of the central tube is communicated with the synthesis gas inlet, a plurality of distribution holes penetrating through the tube wall of the central tube are uniformly formed in the tube wall of the central tube, each distribution hole comprises a steady flow section and a diffusion section, the steady flow section is of a cylindrical hole structure, and the diffusion section is of an externally expanded horn mouth structure; and the catalyst bed layer is arranged in the reaction cavity between the central pipe and the shell. According to the application, the distribution holes adopt a horn mouth structure of a flow stabilizing section and a diffusion section, so that the blocking risk of catalyst particles and impurities is effectively reduced; meanwhile, the spherical structure of the dispersing head, the central airflow channel and the auxiliary micropores are designed, so that the blockage problem is further avoided, the inlet and outlet pressure difference of the reactor is remarkably reduced, and the production load stability is guaranteed.

Description

Technical Field

[0001] This application relates to the field of methanol production equipment technology, and in particular to an anti-clogging methanol synthesis reactor. Background Technology

[0002] Methanol, as a core raw material in the organic chemical industry, plays an irreplaceable role in numerous industrial sectors such as pharmaceuticals, pesticides, dyes, synthetic fibers, synthetic resins, and synthetic plastics. It is also a key intermediate product in modern coal chemical industry and a vehicle fuel with significant development potential. Currently, global methanol synthesis plants are rapidly developing towards large-scale, low-energy-consumption, and environmentally friendly designs. my country's methanol industry not only faces fierce domestic market competition but also endures severe competition from imported methanol. Against this backdrop, effectively increasing methanol yield and reducing production costs have become crucial for enhancing the core competitiveness of enterprises.

[0003] In existing million-ton-level methanol production enterprises in China, the synthesis reactor is the core equipment in the methanol synthesis process, and its internal central tube, as a major internal component, is the core technology of the entire reactor. The central tube is usually a hollow, vertical, axially cylindrical pipe installed in the center of the synthesis tower. The process synthesis gas enters the gas distribution cylinder from the lower part or both the upper and lower parts of the central tube. After distribution, it enters the catalyst bed radially to react and produce methanol, releasing a large amount of heat. The generated methanol gas then enters the cooling system. Boiler water enters the heat exchange tube from the lower main pipe, absorbs the heat released by the reaction, and then flows out from the upper main pipe into the steam drum, realizing heat recovery.

[0004] However, existing central tubes and their associated synthesis reactors have many shortcomings, which severely restrict their application in large-scale methanol synthesis plants:

[0005] Frequent blockages occur during methanol production. The small holes in the central tube are easily blocked by catalyst particles and impurities in the feed gas, leading to an increase in the pressure difference between the inlet and outlet of the synthesis reactor and a decrease in production load. In severe cases, it can even force companies to shut down for maintenance in advance, disrupting the normal production rhythm.

[0006] Maintenance costs are high. After the small holes become clogged, a lot of manpower, material resources and time are needed to manually unclog them. Even after they are unclogged and put back into use, the clogging problem will recur, forming a vicious cycle that seriously affects the company's production efficiency. Summary of the Invention

[0007] This application provides an anti-clogging methanol synthesis reactor to solve the problem in the prior art where the distribution holes in the central tube are easily clogged by catalyst particles and impurities in the feed gas.

[0008] This application provides an anti-clogging methanol synthesis reactor, comprising:

[0009] The shell contains a reaction chamber, and the shell has a synthesis gas outlet that communicates with the reaction chamber.

[0010] The central tube is set in the reaction chamber. The end of the central tube is connected to the synthesis gas inlet. Multiple distribution holes are evenly opened on the tube wall of the central tube. Each distribution hole includes a flow stabilizing section and a diffusion section. The flow stabilizing section has a cylindrical hole structure, and the diffusion section has an outwardly expanding funnel-shaped structure.

[0011] The catalyst bed is located in the reaction chamber between the central tube and the shell.

[0012] In one possible design, the angle between the inner wall of the diffuser section and its central axis is α, where 10°≤α≤45°.

[0013] In one possible design, the depth of the diffuser section is less than or equal to 1 / 3 of the wall thickness of the central tube.

[0014] In one possible design, multiple dispersing heads are also included, each corresponding to a distribution hole. Each dispersing head includes an end cap and a connecting body. The end cap is positioned opposite to the distribution hole. One end of the connecting body is connected to the central tube, and the other end is connected to the end cap. A dispersing port communicating with the distribution hole is formed on the connecting body.

[0015] In one possible design, an airflow channel is provided in the center of the end cap.

[0016] In one possible design, the end cap away from the central tube is spherical, and multiple auxiliary micropores are formed on the spherical surface around the airflow channel.

[0017] In one possible design, the connector consists of at least two connecting rods, with the outer ends of the connecting rods connected to the end caps and passing through the distribution holes and connecting to the central tube.

[0018] In one possible design, the inner end of the connecting rod is bent at 80°-100° and then welded to the inner wall of the central tube.

[0019] In one possible design, the central tube consists of multiple segments, with adjacent segments connected detachably using a socket structure.

[0020] In one possible design, a heat exchange tube bundle is also included. The heat exchange tube bundle is disposed in the reaction chamber between the central tube and the shell and is arranged alternately with the catalyst bed. The heat exchange medium in the heat exchange tube bundle is used to absorb the reaction heat released by the catalyst bed.

[0021] And / or, a top layer of magnetic spheres is provided on the upper part of the catalyst bed, and a bottom layer of magnetic spheres is provided on the lower part of the catalyst bed.

[0022] The beneficial effects of this application are as follows:

[0023] The anti-clogging methanol synthesis reactor of this application adopts a funnel-shaped structure of "stabilizing section + diffuser section" for the central tube distribution holes, combined with a large diameter design of 5mm to 12mm, which effectively reduces the risk of clogging by catalyst particles and impurities. At the same time, the spherical structure of the dispersion head, the central airflow channel and the auxiliary micropore design further avoid clogging problems, significantly reduce the pressure difference between the reactor inlet and outlet, and ensure stable production load.

[0024] The gas distribution uniformity is improved. The funnel-shaped diffuser section, through a gradually expanding channel, suppresses gas flow boundary layer separation and eddy generation, reducing local drag loss by 30% to 60%. At the same time, the Bernoulli equation is used to realize the conversion of dynamic pressure to static pressure, enhancing the gas flow's penetration into the catalyst bed. Combined with the multi-directional dispersion effect of the dispersion head, the gas flow diffuses in a fan shape, expanding the gas-solid contact area, reducing dead zones, and improving reaction efficiency.

[0025] The catalyst is well protected. The end cap of the dispersion head can prevent high-flow-rate synthesis gas from being directly injected into the catalyst bed, thus avoiding catalyst erosion and pulverization. The arrangement of top and bottom magnetic balls further fixes the catalyst bed and extends the catalyst's service life.

[0026] With high structural strength and stability, the depth of the diffuser section is controlled within 1 / 3 of the pipe wall thickness, ensuring the pressure and deformation resistance of the central pipe; the multi-segment socket structure and the bending and welding design of the connecting rod ensure that the equipment is installed firmly, and even under abnormal operating conditions such as syngas backflow, the dispersion head will not fall off, avoiding damage to subsequent pipelines and compressor units.

[0027] The processing and installation are convenient. The diameter of the central tube distribution holes has been increased and the number has been reduced, which lowers the requirements for processing accuracy and manufacturing difficulty, and shortens the processing cycle. The multi-section detachable connection design facilitates the installation, maintenance and replacement of the equipment, and reduces maintenance costs. Attached Figure Description

[0028] To more clearly illustrate the technical solutions in the specific embodiments of this application or the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0029] Figure 1 This is a schematic diagram of the anti-clogging methanol synthesis reactor provided in an embodiment of this application;

[0030] Figure 2 This is a front view of the central tube of the anti-clogging methanol synthesis reactor provided in an embodiment of this application;

[0031] Figure 3A side view of the central tube of the anti-clogging methanol synthesis reactor provided in an embodiment of this application;

[0032] Figure 4 This is a schematic diagram of the distribution holes in the central tube of the anti-clogging methanol synthesis reactor provided in an embodiment of this application;

[0033] Figure 5 This is a front view of the dispersion head of the anti-clogging methanol synthesis reactor provided in an embodiment of this application;

[0034] Figure 6 A side view of the dispersion head of an anti-clogging methanol synthesis reactor provided in an embodiment of this application.

[0035] Figure label:

[0036] 100, Shell; 110, Syngas Inlet; 120, Syngas Outlet; 200, Central Tube; 210, Distribution Hole; 211, Flow Stabilization Section; 212, Diffuser Section; 300, Catalyst Bed; 400, Dispersion Head; 410, End Cap; 411, Gas Flow Channel; 420, Connector; 500, Heat Exchanger Tube Bundle; 610, Top Magnetic Sphere; 620, Bottom Magnetic Sphere. Detailed Implementation

[0037] The technical solutions of this application will be clearly and completely described below with reference to the embodiments. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0038] The following is combined Figures 1-6 This describes the anti-clogging methanol synthesis reactor provided in the embodiments of this application.

[0039] Reference Figure 1 As shown, the anti-clogging methanol synthesis reactor provided in this application embodiment includes a shell 100, a central tube 200, a catalyst bed 300, a dispersion head 400, a heat exchange tube bundle 500, a top magnetic ball 610, and a bottom magnetic ball 620.

[0040] A closed reaction chamber is formed within the shell 100, serving as the space for the methanol synthesis reaction. The shell 100 is provided with a synthesis gas inlet 110 adapted to the central tube 200, and a synthesis gas outlet 120 communicating with the reaction chamber. Synthesis gas enters the reaction chamber through the synthesis gas inlet 110, and the reacted mixture is discharged through the synthesis gas outlet 120. Simultaneously, the shell 100 is also provided with a medium inlet and outlet adapted to the heat exchange tube bundle 500 for the circulation of the heat exchange medium.

[0041] A central tube 200 is positioned at the center of the reaction chamber, with its end connected to the syngas inlet 110. It introduces syngas into the reaction chamber and distributes it to the catalyst bed 300. Multiple distribution holes 210 are uniformly formed through the wall of the central tube 200, each including a flow stabilizing section 211 and a diffuser section 212. Specifically, the flow stabilizing section 211 has a cylindrical hole structure, providing a stable flow channel for the syngas. The diffuser section 212 has an outwardly flared funnel-shaped structure and is located on the outlet side of the distribution hole 210, that is, near the catalyst bed 300.

[0042] In the prior art, the distribution holes are cylindrical. When the airflow flows from the inside of the central cylinder (high pressure side) to the catalyst bed (low pressure side), a "sudden expansion" flow pattern is formed at the outlet of the holes. The outlet edge of the cylindrical holes is right angled. When the airflow passes through, boundary layer separation is easily generated, and the airflow separates from the hole wall, forming a vortex zone. The vortex consumes the kinetic energy of the airflow, resulting in increased resistance.

[0043] In this application, when the airflow enters the diffuser section 212 from the steady flow section 211, the cross-sectional area of ​​the channel gradually increases, avoiding boundary layer separation caused by sudden expansion. The eddy phenomenon is significantly suppressed. The gradual bell mouth can reduce the local resistance of the small hole outlet by 30% to 60%, reduce the energy loss in the process gas flow process, and reduce the risk of blockage from a structural perspective.

[0044] In addition, the process gas has a certain flow velocity (high dynamic pressure) in the central cylinder. When it passes through the diffuser section 212, the channel expansion leads to a decrease in flow velocity (reduction in dynamic pressure). According to Bernoulli's equation, the decrease in dynamic pressure will be converted into an increase in static pressure. After the static pressure is increased, the penetration ability of the gas flow is enhanced. The catalyst bed is a porous medium composed of particle stacking with tiny gaps inside. The gas flow with higher static pressure can penetrate into the depth of the bed more smoothly, rather than just staying on the surface of the bed.

[0045] Meanwhile, the diffusion effect of the diffuser section 212 increases the diffusion angle of the gas outlet, expands the contact area between the gas flow and the catalyst particles, and reduces the dead angle of gas-solid contact.

[0046] Reference Figure 4 As shown, in some specific embodiments, the angle α between the inner wall of the diffuser section 212 and its central axis satisfies 10°≤α≤45°. This angle range is determined by optimization through reaction space velocity and CFD flow field analysis. The angle range of 10° to 45° achieves a precise balance between the flow diffusion effect and resistance control. If the angle is too small, the resistance cannot be effectively reduced, and if the angle is too large, secondary eddies are easily generated. This range can be matched with the conventional reaction space velocity of methanol synthesis to avoid the problem of insufficient airflow diffusion or a sharp increase in resistance when the space velocity fluctuates, ensuring that the reactor can operate stably under different loads and improving operational flexibility.

[0047] Reference Figure 4 As shown, in some specific embodiments, the depth of the diffuser section 212 is less than or equal to 1 / 3 of the wall thickness of the central tube 200. This ensures the structural strength of the central tube 200 and prevents excessive thinning of the tube wall due to the processing of the diffuser section 212, which would affect its compressive and deformation resistance. This approach guarantees the flow-expanding function of the bell mouth while avoiding excessive thinning of the central tube 200 wall, ensuring that the central tube 200 can withstand the high pressure and catalyst weight within the reactor. It is particularly suitable for the long-term high-pressure operation requirements of large-scale reactors with capacities of millions of tons, improving the structural stability and service life of the equipment and reducing maintenance risks caused by insufficient structural strength.

[0048] In some specific embodiments, the central tube 200 includes multiple cylindrical sections, and adjacent central tube sections 200 are detachably connected by a socket structure, and the splice is fixed by countersunk bolts, which facilitates installation, maintenance and adjustment of concentricity, and adapts to the needs of reactors of different heights.

[0049] In some specific embodiments, the diameter of the distribution holes 210 ranges from 5 mm to 12 mm, with the specific diameter determined according to the specifications of the catalyst used, satisfying a ratio of hole diameter to catalyst diameter of 1.1 to 1.5. The hole spacing of the distribution holes 210 is 14 mm to 18 mm, and the total area of ​​the openings is not less than 100% and not more than 120% of the design area, ensuring both gas flow rate and structural strength of the central tube 200.

[0050] Compared to the existing technology with small holes of 2mm diameter, the large-diameter distribution holes 210 of 5mm to 12mm can effectively avoid clogging by catalyst particles and impurities. The opening ratio is precisely matched with the catalyst diameter, which not only prevents the catalyst from entering the hole, but also ensures gas flow. The reasonable hole spacing of 14mm to 18mm, combined with the total number of openings that is not less than the design area, reduces the number of openings and improves the structural strength of the central tube 200, while ensuring uniform gas distribution, meeting the requirement that the pressure difference between the reactor inlet and outlet is less than 0.025MPa, and improving the stability of production load.

[0051] Reference Figure 2 , Figure 3 , Figure 5 , Figure 6 As shown, in some specific embodiments, a plurality of dispersing heads 400 are also included, each dispersing head 400 being disposed one-to-one with each distribution hole 210. Each dispersing head 400 includes an end cap 410 and a connecting body 420. The end cap 410 is disposed opposite to the distribution hole 210. The connecting body 420 consists of at least two connecting rods, one end of which is connected to the end cap 410, and the other end passes through the distribution hole 210 and is fixedly connected to the inner wall of the central tube 200. A dispersing port communicating with the distribution hole 210 is formed on the connecting body 420, that is, a dispersing port is formed between two adjacent connecting rods, for dispersing the synthesis gas in multiple directions.

[0052] Thus, the end cap 410 of the dispersion head 400 can prevent high-flow-rate syngas from being directly injected into the catalyst bed 300, avoiding catalyst erosion and pulverization, and extending the catalyst's service life. The multi-directional dispersion port allows the syngas to diffuse in a fan shape, expanding the gas-solid contact area, reducing dead zones, and further improving the uniformity of gas distribution. Combined with the diffusion design of the distribution hole 210, it achieves three-stage gas distribution optimization of "stabilization-diffusion-dispersion", contributing to improved reaction efficiency.

[0053] In some specific embodiments, an airflow channel 411 is provided in the center of the end cap 410. The airflow channel 411 is coaxial with the distribution hole 210 and has a diameter of 2 mm to 4 mm. It is used for a small flow rate of synthesis gas to enter the catalyst bed 300 vertically. The central airflow channel 411 can balance the pressure difference on both sides of the dispersion head 400, avoid uneven stress on the equipment due to excessive pressure difference, and play a role in protecting the equipment. On the other hand, the small flow rate of vertical airflow can penetrate into the depth of the catalyst bed 300, supplement the insufficient radial dispersion airflow, further improve the uniformity of gas distribution, ensure reaction stability, and avoid the problem of insufficient reaction in local areas.

[0054] In other specific embodiments, the end cap 410 away from the central tube 200 has a spherical structure. Multiple auxiliary micropores are formed around the airflow channel 411 on the spherical surface of the end cap 410. These auxiliary micropores prevent the central airflow channel 411 from being blocked, thus affecting gas flow. Simultaneously, they balance the force on the end cap 410, ensuring that the airflow is evenly sprayed radially onto the catalyst. The spherical structure design ensures that the catalyst can only block the central airflow channel 411, not the surrounding auxiliary micropores, guaranteeing the continuity of gas flow and preventing localized gas distribution failure caused by blockage of a single channel. The auxiliary micropores further disperse the airflow, ensuring that the airflow evenly covers the catalyst bed 300 radially, balancing the force on the end cap 410, preventing localized deformation or damage caused by high-pressure gas, and improving the structural stability and gas distribution effect of the dispersion head 400.

[0055] Reference Figure 5 , Figure 6 As shown, in some specific embodiments, the inner end of the connecting rod is bent at 80°-100° and then welded to the inner wall of the central tube 200. Full welding is used to ensure a firm connection and prevent the dispersion head 400 from detaching when syngas flows back. The method of full welding after bending the connecting rod ensures that the dispersion head 400 faces the direction of syngas flow during normal operation, making the connection more secure. Under abnormal operating conditions such as syngas backflow, it will not detach, preventing the dispersion head 400 from entering the central tube 200 or the compressor unit and causing equipment damage. This comprehensively improves the mechanical properties of the central tube 200 and the operational safety of the reactor, ensuring long-term stable operation of the equipment.

[0056] Furthermore, the connecting rod is 15mm to 20mm long, with a bent section at its end (5mm to 8mm) facing towards the inner wall of the central tube 200. This bend towards the inner wall allows the welding point to fit more closely to the inner wall of the central tube 200, reducing interference with airflow within the tube. It also facilitates insertion and fixing from the inside of the central tube 200 during installation, improving ease of installation.

[0057] The catalyst bed 300 is located in the reaction chamber between the central tube 200 and the shell 100, and is formed by the accumulation of particulate catalyst. It provides a catalytic environment for the reaction of syngas to methanol. The heat exchange tube bundle 500 is located in the reaction chamber between the central tube 200 and the shell 100, and is arranged alternately with the catalyst bed 300. A heat exchange medium (such as boiler water) flows in the heat exchange tube bundle 500 to absorb the heat released by the reaction in the catalyst bed 300, thereby achieving stable control of the bed temperature. At the same time, it recovers heat to generate steam, realizing energy reuse.

[0058] The heat exchange tube bundle 500 can promptly remove the large amount of heat released by the methanol synthesis reaction, avoiding the risk of catalyst activity decay or overheating due to excessively high bed temperature, while preventing the reaction rate from being affected by excessively low temperature, ensuring that the bed temperature is stable within the optimal range; the absorbed heat heats the boiler water to generate steam, realizing energy recovery and reuse, reducing the energy consumption of the unit, which is in line with the low-energy consumption development direction of the methanol industry and improves the economic benefits of enterprises.

[0059] The top layer magnetic spheres 610 are positioned on the upper part of the catalyst bed 300, and the bottom layer magnetic spheres 620 are positioned on the lower part of the catalyst bed 300. Both are made of high-strength, high-temperature-resistant magnetic material with a particle size larger than the catalyst particles. The bottom layer magnetic spheres 620 support the catalyst bed 300, bearing the weight of the catalyst and preventing it from settling and leaking. The top layer magnetic spheres 610 compact and fix the catalyst bed 300 by gravity, preventing catalyst fluidization or loss due to airflow impact. The magnetic properties and porous structure of both spheres can intercept impurities and fine catalyst powder in the syngas, preventing them from clogging the distribution holes 210 of the central tube 200, the dispersion head 400, or entering subsequent systems, thus protecting the equipment, reducing the risk of clogging, and extending the equipment maintenance cycle.

[0060] The working process of the anti-clogging methanol synthesis reactor in this application is as follows:

[0061] Syngas enters the central tube 200 through the syngas inlet 110 and diffuses into the catalyst bed 300 through the distribution holes 210 on the tube wall during its flow inside the central tube 200.

[0062] Specific diffusion path: The syngas first passes through the flow stabilization section 211 of the distribution hole 210 to stabilize its flow rate, and then enters the diffusion section 212 to achieve gradual flow expansion and pressurization. Subsequently, it is sprayed into the catalyst bed 300 in multiple directions and uniformly through the airflow channel 411 of the dispersion head 400, the auxiliary micropores and the dispersion port formed by the connecting rod. Under the catalytic action of the catalyst, the syngas reacts to produce methanol and releases a large amount of heat.

[0063] The boiler water in the heat exchange tube bundle 500 absorbs the heat of reaction and is heated and vaporized. The generated steam enters the steam drum through the steam outlet for recycling. The mixed gas after the reaction passes through the top magnetic ball 610 and is discharged from the reactor through the syngas outlet 120, and enters the subsequent cooling and separation system.

[0064] Throughout operation, the bottom magnetic balls 620 and top magnetic balls 610 intercept impurities and fine catalyst powder in the syngas, preventing blockage of the distribution holes 210 and the dispersing head 400. The end cap 410 of the dispersing head 400 prevents high-speed airflow from directly scouring the catalyst, protecting it from pulverization. The flared structure of the diffuser section 212 reduces airflow resistance, enhances gas penetration, and ensures sufficient gas-solid contact. The multi-segment structure of the central tube 200 and the welded fixing method of the dispersing head 400 ensure long-term stable operation of the equipment and reduce the frequency of downtime for maintenance.

[0065] The anti-clogging methanol synthesis reactor in this embodiment effectively solves the problems of easy clogging of the central tube 200, high processing difficulty, and high maintenance cost in the prior art through the above structural design. It achieves synergistic optimization of uniform gas distribution, catalyst protection, and energy recovery, which can meet the requirements of long-term, efficient, and stable operation of a million-ton-level methanol synthesis unit. At the same time, it realizes the localization of core technologies, significantly improving the economic benefits and market competitiveness of enterprises.

[0066] In the description of this application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc., indicating the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this application.

[0067] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0068] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between components; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise expressly limited. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0069] In this application, the terms "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to a specific feature, structure, material, or characteristic described in connection with that embodiment or example, which is included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0070] Although embodiments of this application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting this application. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of this application.

Claims

1. A clog-resistant methanol synthesis reactor characterized in that, include: A housing, wherein a reaction chamber is formed within the housing, and a synthesis gas outlet communicating with the reaction chamber is provided on the housing; A central tube is disposed in the reaction chamber. The end of the central tube is connected to the synthesis gas inlet. Multiple distribution holes are evenly opened on the tube wall of the central tube, each of which includes a flow stabilizing section and a diffusion section. The flow stabilizing section has a cylindrical hole structure, and the diffusion section has an outwardly expanding funnel-shaped structure. The catalyst bed is disposed in the reaction chamber between the central tube and the shell.

2. The anti-plugging methanol synthesis reactor of claim 1, wherein, The angle between the inner wall of the diffuser section and its central axis is α, where 10°≤α≤45°.

3. The anti-plugging methanol synthesis reactor of claim 2, wherein, The depth of the diffuser section is less than or equal to 1 / 3 of the wall thickness of the central tube.

4. The anti-clogging methanol synthesis reactor according to any one of claims 1-3, characterized in that, It also includes multiple dispersing heads, which are respectively disposed at the distribution holes. Each dispersing head includes an end cap and a connecting body. The end cap is disposed opposite to the distribution hole. One end of the connecting body is connected to the central tube, and the other end is connected to the end cap. A dispersing port communicating with the distribution hole is formed on the connecting body.

5. The anti-plugging methanol synthesis reactor of claim 4, wherein, An airflow channel is provided in the center of the end cap.

6. The anti-plugging methanol synthesis reactor of claim 5, wherein, The end cap away from the central tube is spherical, and multiple auxiliary micropores are formed on the spherical surface around the airflow channel.

7. The anti-plugging methanol synthesis reactor of claim 6, wherein, The connector consists of at least two connecting rods, the outer ends of which are connected to the end caps and pass through the distribution holes and are connected to the central tube.

8. The anti-plugging methanol synthesis reactor of claim 7, wherein, The inner end of the connecting rod is bent at 80°-100° and then welded to the inner wall of the central tube.

9. The anti-plugging methanol synthesis reactor of claim 1, wherein, The central tube comprises multiple segments, and adjacent segments of the central tube are detachably connected by a socket structure.

10. The anti-plugging methanol synthesis reactor of claim 1, wherein, It also includes a heat exchange tube bundle, which is disposed in the reaction chamber between the central tube and the shell and is arranged alternately with the catalyst bed. The heat exchange medium in the heat exchange tube bundle is used to absorb the reaction heat released by the catalyst bed. And / or, the upper part of the catalyst bed is provided with top layer magnetic spheres, and the lower part of the catalyst bed is provided with bottom layer magnetic spheres.

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