Gas distributor, fluidized bed reactor and hydrocarbon ammoxidation reaction method

Abstract

The present application relates to the technical field of chemical industry, disclose a kind of gas distributor, fluidized bed reaction device and hydrocarbon ammoxidation reaction method, gas distributor includes base frame and multiple gas distribution mechanisms, base frame includes main gas inlet pipe and multiple branch pipes distributed along the circumference of main gas inlet pipe, branch pipe is communicated with main gas inlet pipe, main gas inlet pipe is provided with main gas inlet for gas entering;Multiple gas distribution mechanisms are respectively arranged in corresponding branch pipe, gas distribution mechanism includes multiple pairs of distribution pipes distributed along the axial direction of branch pipe, distribution pipe is communicated with branch pipe, in the direction of gas flow in corresponding branch pipe, the pair of distribution pipe is symmetrically arranged on the two sides of branch pipe;Distribution pipe includes multiple distribution cavities distributed along the axial direction of distribution pipe and communicated with each other, distribution cavity is provided with spout for gas ejection, the top surface of distribution cavity is tapered in the direction of gas flow in distribution pipe.Through the setting of barb-shaped distribution pipe, the gas distribution uniformity of gas distributor is improved.

Description

Technical Field

[0001] This invention relates to the field of chemical engineering technology, specifically to a gas distributor, a fluidized bed reactor, and a method for hydrocarbon ammonia oxidation reaction. Background Technology

[0002] A gas distributor is a device that ensures the uniform distribution of gas across the cross-section of a reactor. It is a crucial component of a gas-solid fluidized bed reactor, serving two main functions: firstly, to uniformly distribute fluidizing air to maintain the fluidized state of the fluidized bed; and secondly, to provide the gas for the reaction to ensure the process can proceed. Therefore, the gas distribution performance of the distributor directly affects the operation of the fluidized bed.

[0003] Taking tubular distributors as an example, they are commonly used in aromatic ammonia oxidation and acrylonitrile fluidized bed reactors. Currently, tubular distributors have multiple evenly distributed branches, each with multiple evenly distributed nozzles, using straight pipes as branches. However, using conventional tubular distributors still results in a typical variable mass flow field internally, with relatively uneven gas distribution. Furthermore, this unevenness increases with the increase in reactor diameter. Summary of the Invention

[0004] The purpose of this invention is to overcome the problem of uneven gas distribution in existing gas distributors and to provide a gas distributor having a barbed distribution tube, thereby improving the uniformity of gas distribution.

[0005] To achieve the above objectives, the present invention provides a gas distributor, the gas distributor comprising:

[0006] A base frame, comprising a main intake pipe and a plurality of branch pipes circumferentially distributed along the main intake pipe, the branch pipes being connected to the main intake pipe, and the main intake pipe having a main intake port for gas entry; and

[0007] Multiple gas distribution mechanisms are provided, each of which is disposed in a corresponding branch pipe. Each gas distribution mechanism includes multiple pairs of distribution pipes distributed axially along the branch pipe, the distribution pipes being connected to the branch pipe. In the airflow direction within the corresponding branch pipe, the pairs of distribution pipes are symmetrically arranged on both sides of the branch pipe; wherein:

[0008] The distribution pipe includes a plurality of distribution cavities that are distributed along the axial direction of the distribution pipe and are interconnected with each other. Each distribution cavity is provided with a nozzle for gas ejection, and the top surface of the distribution cavity is tapered in the direction of airflow within the distribution pipe.

[0009] The above technical solution, by setting the distribution pipe in the branch pipe to have multiple distribution cavities that are distributed along the axial direction of the distribution pipe and are interconnected with each other, and by making the top surface of the distribution cavity gradually narrow along the airflow direction in the distribution pipe, can make the gas to be distributed uniformly, thereby greatly improving the gas distribution uniformity of the gas distributor.

[0010] Preferably, in the direction of airflow within the distribution pipe, both longitudinal openings of the distribution cavity opposite to each other are circular; and / or

[0011] Along the airflow direction within the distribution tube, the two opposing longitudinal openings of the distribution cavity are a first longitudinal opening and a second longitudinal opening, respectively, and the ratio of the area of ​​the longitudinal section where the second longitudinal opening is located to the area of ​​the longitudinal section where the first longitudinal opening is located is (0.1-0.9):1.

[0012] Preferably, the gas distributor includes a flow disruptor disposed within the corresponding distribution cavity.

[0013] Preferably, the turbulence diffuser includes a turbulence body disposed in the corresponding distribution cavity. The turbulence body includes a first turbulence portion and a second turbulence portion that can be combined with the first turbulence portion. The first turbulence portion has a material-facing surface, and the second turbulence portion has a material-returning surface that is opposite to the material-facing surface and connected to the material-facing surface. The material-facing surface and the material-returning surface can together enclose and form the outer contour of the turbulence body.

[0014] Wherein: the receiving surface is a first arc-shaped surface convex toward the turbulent body, and the back surface is a second arc-shaped surface convex toward the turbulent body.

[0015] Preferably, the arc length corresponding to the chord length connecting the top and bottom of the first arc surface is the first arc length, and the arc length corresponding to the chord length connecting the top and bottom of the second arc surface is the second arc length; wherein: the first arc length is greater than the second arc length.

[0016] Preferably, along the airflow direction within the distribution tube, the two opposing longitudinal openings of the distribution cavity are a first longitudinal opening and a second longitudinal opening, respectively.

[0017] The ratio of the area of ​​the longitudinal section of the first spoiler to the area of ​​the first longitudinal opening is (0.15-0.45):1; and / or

[0018] The ratio of the area of ​​the longitudinal section of the second spoiler to the area of ​​the first longitudinal opening is (0.15-0.45):1.

[0019] Preferably, the angle between the chord length connecting the top and bottom of the first arcuate surface and the bottom surface of the distribution cavity is 15°-60°; and / or

[0020] The angle between the chord length connecting the top and bottom of the second arcuate surface and the bottom surface of the distribution cavity is 30°-75°.

[0021] Preferably, the distribution cavity is provided with a pair of nozzles for gas ejection, and in the horizontal direction perpendicular to the airflow direction of the distribution pipe, the pair of nozzles are respectively located on both sides of the corresponding turbulence body;

[0022] The gas distribution mechanism includes a pair of nozzles respectively assembled in the same distribution cavity of the corresponding nozzles.

[0023] Preferably, the nozzles are arranged at an angle, and in the direction from the top surface of the distribution cavity to the bottom surface of the distribution cavity, the pairs of nozzles gradually move away from each other.

[0024] Preferably, in the direction of airflow within the distribution tube, a pair of nozzles are staggered, and the two opposing longitudinal openings of the distribution cavity are a first longitudinal opening and a second longitudinal opening, respectively.

[0025] The pair of nozzles are a first nozzle near the first longitudinal opening and a second nozzle near the second longitudinal opening, wherein: the ratio of the distance between the first arcuate surface and the second nozzle to the diameter of the second longitudinal opening is 0.25-0.85, and the ratio of the distance between the second arcuate surface and the second nozzle to the diameter of the second longitudinal opening is 0.2-0.75.

[0026] A second aspect of the present invention provides a fluidized bed reactor, the fluidized bed reactor comprising a reaction shell and a gas distributor provided by the present invention disposed within the reaction shell, the gas distributor being disposed along a height direction perpendicular to the reaction shell;

[0027] The fluidized bed reactor further includes an air distributor arranged perpendicular to the height of the reaction shell and located below the gas distributor, and a catalyst layer filled within the reaction shell, wherein the nozzle faces the air distributor. By providing a gas distributor within the reaction shell, the gas used for the reaction can be evenly distributed, thereby improving the reaction effect and efficiency.

[0028] A third aspect of the present invention provides a method for hydrocarbon ammonia oxidation reaction, wherein the hydrocarbon ammonia oxidation reaction is carried out using a fluidized bed reactor provided by the present invention, the method comprising:

[0029] Step S00: Hydrocarbons and ammonia are introduced into the gas distributor, causing the gas distributor to spray the hydrocarbons and ammonia toward the air distributor;

[0030] Step S20: Use the air distributor to distribute air within the reaction vessel;

[0031] Step S40: The hydrocarbon, ammonia, and air undergo an ammonia oxidation reaction in the presence of a catalyst to obtain a nitrile.

[0032] Preferably, in step S40, the reaction temperature of the ammonia oxidation reaction is 320℃-500℃, and the reaction pressure is 0.01MPa-0.15MPa; and / or

[0033] The molar ratio of hydrocarbons, ammonia and air is 1:(1-10):(8-40).

[0034] Preferably, the uniformity of gas distribution by the gas distributor is P, where P = 1 - M, and M is calculated using the following formula:

[0035] Where n is the number of nozzles in the gas distributor, u i This refers to the injection flow rates of hydrocarbons and ammonia ejected from the corresponding nozzles. It is the average jet flow rate of n nozzles. Attached Figure Description

[0036] Figure 1 This is a cross-sectional structural schematic diagram of a fluidized bed reactor according to a preferred embodiment of the present invention, wherein a gas distributor according to a preferred embodiment of the present invention is installed.

[0037] Figure 2 This is a top view of the gas distributor according to a preferred embodiment of the present invention;

[0038] Figure 3 This is a schematic cross-sectional view of the distribution pipe in a gas distributor according to a preferred embodiment of the present invention.

[0039] Figure 4 yes Figure 3 The diagram shows a partial structural schematic of the distribution tube located in a distribution cavity.

[0040] Explanation of reference numerals in the attached figures

[0041] 10-Gas distributor; 12-Base frame; 120-Main air inlet pipe; 122-Branch pipe; 14-Gas distribution mechanism; 140-Distribution pipe; 140a-Distribution cavity; 141-Top surface; 143-Bottom surface; 142-First longitudinal opening; 144-Second longitudinal opening; 16-Breaker; 160-Breaker body; 160a-Feeding surface; 160b-Backing surface; 18-Nozzle; 18a-First nozzle; 18b-Second nozzle; 20-Fluidized bed reactor; 22-Reaction shell; 24-Air distributor; 26-Cyclone separator; 28-Heat exchanger; 29a-Main air pipe; 29b-Guide pipe. Detailed Implementation

[0042] In this invention, unless otherwise stated, directional terms such as "up," "down," "left," and "right" are generally understood in conjunction with the accompanying drawings and the orientation shown in actual application, while "inner" and "outer" refer to the inner and outer contours of the component.

[0043] This invention provides a gas distributor, such as Figure 2 As shown, the gas distributor 10 includes a base frame 12 and a plurality of gas distribution mechanisms 14.

[0044] The base frame 12 includes a main intake pipe 120 and a plurality of branch pipes 122 distributed circumferentially along the main intake pipe 120. The branch pipes 122 can be evenly distributed circumferentially along the main intake pipe 120 and can be vertically installed in the main intake pipe 120. The branch pipes 122 are connected to the main intake pipe 120. The main intake pipe 120 is provided with a main intake port for gas to enter the main intake pipe 120. A plurality of gas distribution mechanisms 14 are respectively installed in the corresponding branch pipes 122. The gas distribution mechanism 14 includes a plurality of branch pipes 122 distributed circumferentially along the main intake pipe 120. A plurality of pairs of distribution pipes 140 are axially distributed in the branch pipe 122. The distribution pipes 140 are connected to the branch pipe 122 and can be vertically installed in the branch pipe 122. Along the airflow direction within the corresponding branch pipe 122, the pairs of distribution pipes 140 are symmetrically arranged on both sides of the branch pipe 122. When the gas to be distributed enters the corresponding branch pipe 122, along the airflow direction within the branch pipe 122, the gas to be distributed can enter the plurality of pairs of distribution pipes 140 corresponding to that branch pipe 122; combined with Figure 3 As shown, the distribution pipe 140 includes a plurality of distribution cavities 140a distributed along the axial direction of the distribution pipe 140 and interconnected with each other. It can be understood that, in conjunction with Figure 4As shown, the two ends of the distribution cavity 140a are open, forming a first longitudinal opening 142 and a second longitudinal opening 144 respectively. Multiple distribution cavities 140a are interconnected to form a corresponding distribution pipe 140. The distribution cavity 140a is provided with a nozzle for gas ejection. In order to eject more stably, a nozzle can be provided at the nozzle. This part will be explained in the following content and will not be repeated here. The top surface 141 of the distribution cavity 140a is gradually narrowed in the airflow direction in the distribution pipe 140. That is to say, the top surface 141 of the distribution cavity 140a gradually approaches the bottom surface 143 of the distribution cavity 140a in the airflow direction in the distribution pipe 140. It can be understood that the top surface 141 of the distribution pipe 140 is barbed in the airflow direction in the distribution pipe 140. The longitudinal cross section of a single distribution cavity 140a is trapezoidal. By configuring the distribution pipe 140 provided in the branch pipe 122 to have multiple distribution cavities 140a that are distributed along the axial direction of the distribution pipe 140 and connected to each other, and making the top surface 141 of the distribution cavity 140a gradually narrow in the airflow direction in the distribution pipe 140, the gas to be distributed can be evenly distributed, which greatly improves the uniformity of gas distribution of the gas distributor 10.

[0045] It should be noted that the gas to be distributed can enter the main intake pipe 120 from the main intake port, and then be distributed to each branch pipe 122. During the flow of the gas along the branch pipe 122, the gas to be distributed will enter each pair of distribution pipes 140 respectively. After that, during the flow of the gas along the corresponding distribution pipe 140, the gas to be distributed will be discharged from the nozzle of the corresponding distribution cavity 140a.

[0046] To further improve the uniformity of air distribution, on the same branch pipe 122, in the direction of airflow within the branch pipe 122, the lengths of multiple distribution pipes 140 located on the same side gradually increase and then gradually decrease.

[0047] Along the airflow direction within the distribution pipe 140, the two opposing longitudinal openings of the distribution cavity 140a are both circular. The two opposing longitudinal openings of the distribution cavity 140a can be a first longitudinal opening 142 and a second longitudinal opening 144, respectively. Thus, both the first longitudinal opening 142 and the second longitudinal opening 144 can be circular. It can be understood that the first longitudinal opening 142 of one distribution cavity 140a and the second longitudinal opening 144 of the other distribution cavity 140a are connected to each other.

[0048] Along the airflow direction within the distribution pipe 140, the two opposing longitudinal openings of the distribution cavity 140a can be a first longitudinal opening 142 and a second longitudinal opening 144, respectively. The area ratio of the second longitudinal section containing the second longitudinal opening 144 to the area of ​​the first longitudinal section containing the first longitudinal opening 142 is (0.1-0.9):1. This means that the area of ​​the second longitudinal section : the area of ​​the first longitudinal section = (0.1-0.9):1. By setting the area ratio of the second longitudinal section to the first longitudinal section within the above range, the distribution cavity 140a can have a reasonable structure, further improving the air distribution effect.

[0049] Combination Figure 3 and Figure 4 As shown, a flow disruptor 16 can be provided in the corresponding distribution cavity 140a to disturb the airflow, thereby making the gas distribution more uniform and further improving the gas distribution uniformity of the gas distributor 10.

[0050] The flow disruptor 16 may include a flow disruptor body 160 disposed within a corresponding distribution cavity 140a. The flow disruptor body 160 may include a first flow disruptor portion and a second flow disruptor portion capable of being joined with the first flow disruptor portion. The first flow disruptor portion may be configured to have a receiving surface 160a, and the second flow disruptor portion may be configured to have a receiving surface 160b facing away from and connected to the receiving surface 160a. The receiving surface 160a and the receiving surface 160b can together enclose and form the outer contour of the flow disruptor body 160. By configuring the flow disruptor 16 to have a first arcuate surface and a second arcuate surface that can be joined with each other, the gas can be effectively disturbed, and the overall structure of the flow disruptor 16 is simple.

[0051] It should be noted that the arc length corresponding to the chord length connecting the top and bottom of the first arc surface is the first arc length, and the arc length corresponding to the chord length connecting the top and bottom of the second arc surface is the second arc length. In order to further improve the turbulence effect, the first arc length can be set to be greater than the second arc length.

[0052] The ratio of the longitudinal cross-sectional area of ​​the first turbulence section to the area of ​​the first longitudinal opening 142 is (0.15-0.45):1, meaning the ratio of the longitudinal cross-sectional area of ​​the first turbulence section to the area of ​​the first longitudinal opening 142 is (0.15-0.45):1. This ensures that the first turbulence section has a reasonable size and can effectively turbulent the gas flowing through the turbulence diffuser 16. In addition, the ratio of the longitudinal cross-sectional area of ​​the second turbulence section to the area of ​​the first longitudinal opening 142 is (0.15-0.45):1, meaning the ratio of the longitudinal cross-sectional area of ​​the second turbulence section to the area of ​​the first longitudinal opening 142 is (0.15-0.45):1. This further ensures the size of the first turbulence section and also further ensures the turbulence effect of the turbulence diffuser 16.

[0053] The angle between the chord length connecting the top and bottom of the first arc-shaped surface and the bottom surface 143 of the distribution cavity 140a can be set to 15°-60°, thus giving the first arc-shaped surface a reasonable curvature. In addition, the angle between the chord length connecting the top and bottom of the second arc-shaped surface and the bottom surface 143 of the distribution cavity 140a can be set to 30°-75°, thus giving the second arc-shaped surface a reasonable curvature.

[0054] A pair of nozzles can be provided on the distribution cavity 140a. In the horizontal direction perpendicular to the airflow direction of the distribution pipe 140, the pair of nozzles can be located on both sides of the corresponding turbulence body 160b. The gas distribution mechanism 14 can include a pair of nozzles 18 respectively assembled to the corresponding nozzles of the same distribution cavity 140a. That is, the pair of nozzles 18 can be respectively assembled to the corresponding nozzles of the same distribution cavity 140a. By providing nozzles 18 at the corresponding nozzles, the gas can be ejected more effectively and stably.

[0055] The nozzles 18 can be tilted, and in the direction from the top surface 141 of the distribution cavity 140a to the bottom surface 143 of the distribution cavity 140a, the pairs of nozzles 18 gradually move away from each other. It can be understood that the pairs of nozzles 18 are in a figure-eight shape.

[0056] Along the airflow direction within the distribution pipe 140, a pair of nozzles are staggered. Therefore, it can be understood that the pair of nozzles 18 can be staggered and arranged, and the two opposing longitudinal openings of the distribution cavity 140a can be respectively set as a first longitudinal opening 142 and a second longitudinal opening 144; combined with... Figure 3 and Figure 4 As shown, a pair of nozzles 18 can be a first nozzle 18a near the first longitudinal opening 142 and a second nozzle 18b near the second longitudinal opening 144, wherein: the ratio of the distance between the first arcuate surface and the second nozzle 18b to the diameter of the second longitudinal opening 144 can be set to 0.25-0.85, and the ratio of the distance between the second arcuate surface and the second nozzle 18b to the diameter of the second longitudinal opening 144 can be set to 0.2-0.75. In this way, the deflector 16 can be reasonably arranged between the corresponding pairs of nozzles 18, and the deflection effect of the deflector 16 can be guaranteed at the same time.

[0057] The present invention also provides a fluidized bed reactor, such as Figure 1As shown, the fluidized bed reactor 20 includes a reaction shell 22 and a gas distributor 10 provided by the present invention disposed within the reaction shell 22. The gas distributor 10 is disposed along a height direction perpendicular to the reaction shell 22. It can be understood that the gas distributor 10 can be disposed laterally within the reaction shell 22. The fluidized bed reactor 20 also includes an air distributor 24 disposed along a height direction perpendicular to the reaction shell 22 and located below the gas distributor 10, and a catalyst layer filled within the reaction shell 22. Specifically, the air distributor 24 can be disposed laterally within the reaction shell 22, and the catalyst layer is located substantially in the lower middle part of the reaction shell 22. The nozzle faces the air distributor 24. It can be understood that when a nozzle 18 is installed at the nozzle, the nozzle 18 can spray gas substantially towards the air distributor 24. By distributing the gas distributor 10 within the reaction shell 22, the gas used for the reaction can be evenly distributed, thereby improving the reaction effect and efficiency.

[0058] To further improve the reaction effect and efficiency, the distance between the gas distributor 10 and the air distributor 24 is 0.01-0.1 times the height of the reaction shell 22.

[0059] It should be noted that a main gas pipe 29a can be inserted into the reaction shell 22, with one end of the main gas pipe 29a connected to the main air inlet pipe 120 to guide gas into the gas distributor 10. The main gas pipe 29a can be located above the gas distributor 10. Additionally, an air guide pipe 29b for introducing air can be inserted into the reaction shell 22. The air guide pipe 29b can be positioned below the air distributor 24. After the air is introduced into the reaction shell 22 through the air guide pipe 29b, it can be evenly distributed through the air distributor 24. The air distributor 24 can be a porous plate with multiple evenly distributed holes.

[0060] In addition, a cyclone separator 26 can be installed inside the reaction shell 22. The cyclone separator 26 can be installed above the gas distributor 10 to separate the products obtained from the reaction, thereby separating the catalyst particles carried in the reaction products. The reaction products are then discharged from the discharge port of the reaction shell 22.

[0061] A heat exchanger 28 can be installed inside the reaction shell 22. The heat exchanger 28 can be positioned above the gas distributor 10, and it can cool the material flowing through it. The structure of the heat exchanger 28 can be selected according to actual needs, as long as it can cool the material.

[0062] The present invention also provides a method for hydrocarbon ammonia oxidation reaction, wherein the hydrocarbon ammonia oxidation reaction is carried out using the fluidized bed reactor 20 provided by the present invention, and the hydrocarbon ammonia oxidation reaction method includes:

[0063] Step S00: Hydrocarbons and ammonia are introduced into the gas distributor 10. Specifically, vaporized hydrocarbons and ammonia can be introduced into the gas distributor 10, causing the gas distributor 10 to spray hydrocarbons and ammonia toward the air distributor 24. It can be understood that the vaporized hydrocarbons and ammonia can enter the air distributor 24 through the main gas pipe 29a, and then be sprayed out by each nozzle 18. The hydrocarbons can be aromatics and / or olefins, wherein the aromatics can be m-xylene and the olefins can be propylene.

[0064] Step S20: Air is distributed in the reaction shell 22 using air distributor 24. It can be understood that the air can first be introduced into the reaction shell 22 through air guide pipe 29b, and then evenly distributed in the reaction shell 22 by air distributor 24. The evenly distributed air can come into contact with the injected hydrocarbons and ammonia.

[0065] Step S40: Hydrocarbons, ammonia, and air undergo an ammonia oxidation reaction under the action of a catalyst to obtain nitrile. The nitrile obtained from the reaction, such as aromatic nitrile, can carry a small amount of catalyst particles and move towards the upper part of the reaction shell 22. After the catalyst particles carried in the nitrile are separated by the cyclone separator 26, the nitrile can be discharged from the discharge port of the reaction shell 22. The nitrile discharged from the fluidized bed reactor 20 can be received by condensation or solvent absorption, and then purified by distillation or recrystallization to obtain product gas.

[0066] In the hydrocarbon ammonia oxidation reaction method, the molar ratio of hydrocarbon, ammonia and air introduced into the fluidized bed reactor 20 is 1:(1-10):(8-40), that is, the number of moles of hydrocarbon: the number of moles of ammonia: the number of moles of air = 1:(1-10):(8-40).

[0067] In step S00 above, the apparent linear velocity of the gas ejected from nozzle 18, i.e., hydrocarbons and ammonia, can be 0.5 m / s to 200 m / s. More preferably, the apparent linear velocity of the ejected gas can be 5 m / s to 100 m / s. Even more preferably, the apparent linear velocity of the ejected gas can be 10 m / s to 50 m / s. It should be noted that the corresponding injection flow rate of nozzle 18 can be calculated based on the apparent linear velocity of the gas ejected from nozzle 18 and the corresponding cross-sectional area of ​​nozzle 18.

[0068] In step S40 above, the reaction temperature of the ammonia oxidation reaction can be controlled at 320℃-500℃, and the reaction pressure of the ammonia oxidation reaction can be controlled at 0.01MPa-0.15MPa.

[0069] The uniformity of gas distribution in gas distributor 10 can be P, where P = 1 - M, and M is calculated using the following formula:

[0070] Where n is the number of nozzles in the gas distributor 10, ui The injection flow rates of hydrocarbons and ammonia ejected from the corresponding nozzles. This is the average jet flow rate of n nozzles. The above calculation method can be used to evaluate the uniformity of gas distribution in the gas distributor 10. The uniformity of gas distribution in the gas distributor 10 of the present invention can reach 0.7 or higher.

[0071] The effects of the present invention will be further illustrated below through examples and comparative examples.

[0072] Example

[0073] Example 1

[0074] use Figure 1 The fluidized bed reactor 20 shown performs an aromatic ammonia oxidation reaction. A gas distributor 10 provided by the present invention is provided inside the reaction shell 22. An air distributor 24 is located below the gas distributor 10. The distance between the air distributor 24 and the gas distributor 10 is 0.05 of the height of the reaction shell 22. A heat exchanger 28 and a cyclone separator 26 are both located above the gas distributor 10.

[0075] Among them, the present invention is used Figure 2 The gas distributor 10 shown has four circumferentially distributed branch pipes 122 on the main intake pipe 120. Six pairs of distribution pipes 140 are provided on the branch pipes 122. Each distribution pipe 140 is composed of multiple distribution cavities 140a that are distributed along the axial direction of the distribution pipe 140 and are interconnected with each other. Each distribution cavity 140a is provided with a pair of nozzles 18, namely the first nozzle 18a and the second nozzle 18b. The area of ​​the second longitudinal section is 0.25:1. The angle between the chord length connecting the top and bottom of the first arc-shaped surface and the bottom surface 143 of the distribution cavity 140a is 30°. The angle between the chord length connecting the top and bottom of the second arc-shaped surface and the bottom surface 143 of the distribution cavity 140a is 50°.

[0076] Aromatic hydrocarbons and ammonia are introduced into the gas distributor 10, causing the gas distributor 10 to spray the aromatic hydrocarbons and ammonia towards the air distributor 24; the air distributor 24 is used to distribute air within the reaction shell 22; after the aromatic hydrocarbons, ammonia, and air come into contact, they undergo an ammonia oxidation reaction under the action of a catalyst to obtain aromatic nitrile; the corresponding aromatic nitrile, carrying the catalyst, leaves the dense phase zone located in the middle and lower part of the reaction shell 22, and the catalyst particles are separated by a cyclone separator 26. The aromatic nitrile is discharged from the fluidized bed reactor and is received by condensation or solvent absorption, etc., and then purified by distillation or recrystallization to obtain product gas, while the separated catalyst re-enters the dense phase zone; wherein, the reaction raw materials are m-xylene, ammonia, and air, the molar ratio of m-xylene, ammonia, and air is m-xylene: ammonia: air = 1:6:22.4, the reaction temperature is 405℃, and the apparent linear velocity of the sprayed xylene and ammonia is 0.5m / s. Calculations show that the uniformity of gas distribution in gas distributor 10 is 0.74, and the yield of isophthalonitrile is 82.4%.

[0077] Comparative Example

[0078] Comparative Example 1

[0079] The process was essentially the same as the previous example, except that a conventional gas distributor 10 was used, and the reactants in the dense phase zone of the fluidized bed reactor were m-xylene, ammonia, and air in a molar ratio of 1:6.4:26.7. The reaction temperature was 420°C, and the apparent linear velocity of the injected gas was 0.5 m / s. All other conditions remained the same. Calculations showed that the uniformity of gas distribution using the gas distributor 10 was 0.56, and the isophthalonitrile yield was 79.4%.

[0080] The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various specific technical features in any suitable manner. To avoid unnecessary repetition, the present invention will not describe the various possible combinations separately. However, these simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A gas distributor, characterized in that, The gas distributor (10) includes: A base frame (12) includes a main intake pipe (120) and a plurality of branch pipes (122) circumferentially distributed along the main intake pipe (120), the branch pipes (122) being connected to the main intake pipe (120), and the main intake pipe (120) being provided with a main intake port for gas entry; and Multiple gas distribution mechanisms (14) are respectively disposed in corresponding branch pipes (122). Each gas distribution mechanism (14) includes multiple pairs of distribution pipes (140) distributed axially along the branch pipe (122). The distribution pipes (140) are connected to the branch pipe (122). In the airflow direction within the corresponding branch pipe (122), the pairs of distribution pipes (140) are symmetrically disposed on both sides of the branch pipe (122); wherein: The distribution pipe (140) includes a plurality of distribution cavities (140a) distributed along the axial direction of the distribution pipe (140) and interconnected with each other. Each distribution cavity (140a) is provided with a nozzle for gas ejection. The top surface (141) of each distribution cavity (140a) is tapered in the direction of airflow within the distribution pipe (140). A flow disruptor (16) is provided inside each distribution cavity (140a). The flow disruptor (16) includes a flow disruptor body (160) disposed on the bottom surface (143) of the distribution cavity (140a). The flow disruptor body (160) includes a first flow disruptor and a second flow disruptor that can be combined with the first flow disruptor. The first flow disruptor has a receiving surface (160a), and the second flow disruptor has a surface facing away from the receiving surface (160a). 160a) and connected to the back surface (160b) of the receiving surface (160a), the receiving surface (160a) and the back surface (160b) can together enclose to form the outer contour of the turbulence body (160), the receiving surface (160a) is a first arc-shaped surface protruding outward of the turbulence body (160), the back surface (160b) is a second arc-shaped surface protruding outward of the turbulence body (160), the distribution cavity (140a) is provided with a pair of nozzles for gas ejection, in the horizontal direction perpendicular to the airflow direction of the distribution pipe (140), the pair of nozzles are respectively located on both sides of the corresponding turbulence body (160), in the airflow direction along the distribution pipe (140), the pair of nozzles are staggered.

2. The gas distributor according to claim 1, characterized in that, In the airflow direction within the distribution tube (140), both of the two opposing longitudinal openings of the distribution cavity (140a) are circular; and / or In the airflow direction along the distribution tube (140), the two longitudinal openings of the distribution cavity (140a) that are opposite to each other are the first longitudinal opening (142) and the second longitudinal opening (144), and the ratio of the area of ​​the longitudinal section where the second longitudinal opening (144) is located to the area of ​​the longitudinal section where the first longitudinal opening (142) is located is (0.1-0.9):

1.

3. The gas distributor according to claim 1, characterized in that, The arc length corresponding to the chord length connecting the top and bottom of the first arc surface is the first arc length, and the arc length corresponding to the chord length connecting the top and bottom of the second arc surface is the second arc length; wherein: the first arc length is greater than the second arc length.

4. The gas distributor according to claim 1, characterized in that, In the airflow direction along the distribution tube (140), the two longitudinal openings of the distribution cavity (140a) that are opposite to each other are the first longitudinal opening (142) and the second longitudinal opening (144). The ratio of the area of ​​the longitudinal section of the first spoiler to the area of ​​the first longitudinal opening (142) is (0.15-0.45):1; and / or The ratio of the area of ​​the longitudinal section of the second turbulence part to the area of ​​the first longitudinal opening (142) is (0.15-0.45):

1.

5. The gas distributor according to claim 1, characterized in that, The angle between the chord length connecting the top and bottom of the first arcuate surface and the bottom surface (143) of the distribution cavity (140a) is 15°-60°; and / or The angle between the chord length connecting the top and bottom of the second arcuate surface and the bottom surface (143) of the distribution cavity (140a) is 30°-75°.

6. The gas distributor according to any one of claims 1-4, characterized in that, The gas distribution mechanism (14) includes a pair of nozzles (18) respectively assembled in the same distribution cavity (140a) of the corresponding nozzles.

7. The gas distributor according to claim 6, characterized in that, The nozzles (18) are inclined and the pairs of nozzles (18) gradually move away from each other in the direction from the top surface (141) of the distribution cavity (140a) to the bottom surface (143) of the distribution cavity (140a).

8. The gas distributor according to claim 6, characterized in that, The two longitudinal openings of the distribution cavity (140a) that are opposite to each other are the first longitudinal opening (142) and the second longitudinal opening (144). The pair of nozzles (18) are a first nozzle (18a) near the first longitudinal opening (142) and a second nozzle (18b) near the second longitudinal opening (144), wherein: the ratio of the distance between the first arcuate surface and the second nozzle (18b) to the diameter of the second longitudinal opening (144) is 0.25-0.85, and the ratio of the distance between the second arcuate surface and the second nozzle (18b) to the diameter of the second longitudinal opening (144) is 0.2-0.

75.

9. A fluidized bed reactor, characterized in that, The fluidized bed reactor (20) includes a reaction shell (22) and a gas distributor (10) as described in any one of claims 1-8 disposed within the reaction shell (22), wherein the gas distributor (10) is disposed along a height direction perpendicular to the reaction shell (22); The fluidized bed reactor (20) further includes an air distributor (24) arranged in a height direction perpendicular to the reaction shell (22) and located below the gas distributor (10), and a catalyst layer filled in the reaction shell (22), wherein the nozzle faces the air distributor (24).

10. A method for the ammonia oxidation reaction of hydrocarbons, characterized in that, The method for performing the hydrocarbon ammonia oxidation reaction using the fluidized bed reactor (20) according to claim 9, the method comprising: Step S00: Hydrocarbons and ammonia are introduced into the gas distributor (10), causing the gas distributor (10) to spray the hydrocarbons and ammonia toward the air distributor (24); Step S20: Use the air distributor (24) to distribute air within the reaction shell (22); Step S40: The hydrocarbon, ammonia, and air undergo an ammonia oxidation reaction in the presence of a catalyst to obtain a nitrile.

11. The method for hydrocarbon ammonia oxidation reaction according to claim 10, characterized in that, In step S40, the reaction temperature of the ammonia oxidation reaction is 320℃-500℃, and the reaction pressure is 0.01 MPa-0.15 MPa; and / or The molar ratio of hydrocarbons, ammonia and air is 1:(1-10):(8-40).

12. The method for hydrocarbon ammonia oxidation reaction according to claim 11, characterized in that, The uniformity of gas distribution in the gas distributor (10) is P, where P = 1 - M, and M is calculated using the following formula: Where n is the number of nozzles in the gas distributor (10), u i The injection flow rates of hydrocarbons and ammonia ejected from the corresponding nozzles. It is the average jet flow rate of n nozzles.

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