Internal components and fluidized bed reactors

Abstract

The present application relates to the technical fields of chemical reaction device, and discloses an inner component and a fluidized bed reactor, the inner component comprises a flow guide vane group, the flow guide vane group comprises a first flow guide vane and a second flow guide vane, the first flow guide vane and the second flow guide vane are oppositely inclined relative to a horizontal plane around a horizontal first axis and are oppositely inclined relative to the horizontal plane around a horizontal second axis, the first axis is perpendicular to the second axis, and edges of the first flow guide vane and the second flow guide vane intersect at a point. The inner component formed by the two oppositely twisted and inclined flow guide vanes is difficult to form an air cushion below the flow guide vanes due to the upward movement tendency of the flow guide vanes in each part of the main flow surface of the flow guide vanes caused by the inclination of the flow guide vanes around the first axis and the second axis, thereby preventing the reduction of the effective contact between the gas and the solid and the overall effective space of the fluidized bed caused by the air cushion, and improving the reaction efficiency.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical reaction device, in particular to an inner component and a fluidized bed reactor. BACKGROUND

[0002] Aromatic hydrocarbon ammoxidation refers to the process that ammonia and oxygen or air convert the -CH3 active group in the molecules of methyl aromatic hydrocarbon, heterocyclic aromatic hydrocarbon and other organic matters into -CN under the action of catalyst. The -CN of the product aromatic nitrile has high reactivity, and can be converted into amine, amide, carboxylic acid, aldehyde and other compounds through hydrogenation, hydrolysis, condensation, polymerization, halogenation and other reactions, which are used to produce chemical products such as pesticide, medicine, fuel, building material and insulation material. The reaction process for aromatic hydrocarbon ammoxidation includes fixed bed, fluidized bed and even moving bed. Since the aromatic nitrile is prepared by ammoxidation, which is a strong exothermic reaction, the fluidized bed has the advantage of easy heat removal, and is a more suitable reactor.

[0003] However, in the fluidized bed, the reaction raw material gas and the catalyst solid particles are often not uniformly mixed, which affects the conversion rate of the reaction, reduces the utilization rate of raw materials and increases the difficulty of product separation. Since there are bubbles in the gas-solid mixed medium that move with the medium, these bubbles will cause back mixing of the solid particles in the bed and the reaction gas phase products. At the same time, the uneven residence time distribution of the gas and solid phases in the fluidized bed will cause the intensification of side reactions such as over-oxidation and ammonia burning, significantly reducing the conversion rate of the reaction and the selectivity of the target product aromatic nitrile.

[0004] In view of the above problems, setting an inner component in the fluidized bed reactor is a simple and effective solution. Reasonable addition of the inner component can guide the generation of bubbles, inhibit the growth and coalescence of bubbles, promote the uniform distribution of gas and solid phases, improve the interphase contact efficiency, and weaken the severe pressure pulsation in the bed to make the fluidized bed run stably.

[0005] Patent CN1055916C discloses a hydrocarbon ammoxidation fluidized bed reactor, which is provided with an inner component in the upper part of the fluidized bed reaction zone, including fillers, baffles, louvered plates, screen meshes and the like. Since the reaction gas does not uniformly rise after leaving the catalyst bed, the addition of the inner component in the upper part of the fluidized bed is beneficial to the breaking of unreacted gas bubbles, increases the gas-solid phase mixing, and improves the contact efficiency of the gas and catalyst in the reaction dilute phase zone. The technology uses the secondary reaction in the dilute phase reaction zone to eliminate the unreacted ammonia in the reaction gas, without adding any organic matter. For the ammoxidation process, it can strengthen production, improve reaction efficiency, shorten process flow, reduce environmental pollution, and has great economic benefits.

[0006] In addition, installing vertical components in the fluidized bed is also a commonly used method to improve the flow state and the gas-solid contact efficiency. The vertical components are generally pipe bundles, fins and flat plates arranged vertically. For example, the straight or U-shaped cooling water pipes arranged in the patents CN101954264A and CN102531958A can not only achieve the purpose of effective heat removal, but also improve the fluidization quality, reduce the non-stable fluidization phenomena such as “gas bubble”, “channeling” and “slugging”.

[0007] However, the above two components have the following disadvantages. When the horizontal component is used, the “air cushion” under the component is difficult to break, which affects the reaction efficiency. When the vertical component is used, the “stagnant layer” formed on the surface of the component reduces the mass transfer and heat transfer efficiency.

[0008] In summary, the use of horizontal components or vertical components alone has the unavoidable disadvantage. Therefore, the combination of the two components provides a new way to solve the problems of the fluidized bed caused by the bubble movement, such as the severe bed pressure fluctuation, uneven gas-solid distribution, low interphase contact efficiency, and serious gas and solid particle backmixing. SUMMARY

[0009] The purpose of the present application is to overcome the problems of the prior art, such as the generation of difficult-to-break bubbles in the gas-solid mixed medium in the fluidized bed, the reduction of mass transfer and heat transfer efficiency, the uneven gas-solid distribution, the severe bed pressure fluctuation, the low interphase contact efficiency, and the serious gas and solid particle backmixing. The present application provides an internal component and a fluidized bed reactor.

[0010] In order to achieve the above purpose, the present application provides an internal component, which comprises a guide vane group, the guide vane group comprises first guide vanes and second guide vanes, the first guide vanes and the second guide vanes are oppositely inclined relative to the horizontal plane around a horizontal first axis and oppositely inclined relative to the horizontal plane around a horizontal second axis, the first axis is perpendicular to the second axis, and the edges of the first guide vanes and the second guide vanes intersect at a point.

[0011] Optionally, the inclination angle of the first guide vanes and the second guide vanes relative to the first axis is 15°-75°; and / or, the inclination angle of the first guide vanes and the second guide vanes around the second axis is 0°-60°.

[0012] Optionally, the first guide vanes and the second guide vanes are provided with through holes; and / or, the first guide vanes and the second guide vanes comprise a plurality of through holes, and the through holes are arranged in an array on the main flow surface of the first guide vanes and the second guide vanes.

[0013] Optionally, the inner member further comprises a vertically arranged support rod, and a plurality of groups of the guide vanes are arranged on the support rod in a vertical direction, and the first guide vanes and the second guide vanes of two adjacent groups of the guide vanes are oppositely inclined around the second axis.

[0014] Optionally, the first guide vanes and the second guide vanes are plate structures, and the vanes are one of trapezoidal, triangular and rectangular, and / or the first guide vanes and the second guide vanes have the same shape.

[0015] The second aspect of the present application provides a fluidized bed reactor, comprising a dilute phase zone and a dense phase zone arranged in sequence along an axial direction of the fluidized bed reactor, and the dense phase zone is provided with the inner member described in the technical solution.

[0016] Optionally, the fluidized bed reactor further comprises a plurality of heat extraction pipes arranged in the dense phase zone, and a plurality of the inner members are arranged in the intervals of the heat extraction pipes.

[0017] Optionally, the fluidized bed reactor further comprises a horizontal support connected between the inner member and the heat extraction pipe.

[0018] Optionally, the fluidized bed reactor further comprises an interface influencing zone between the dilute phase zone and the dense phase zone, and a conical member arranged in the interface influencing zone, and the tip of the conical member is downward.

[0019] Optionally, a plurality of the conical members are arranged in an array in a horizontal direction to form a conical member unit, and the fluidized bed reactor comprises a plurality of the conical member units arranged in a vertical direction.

[0020] Through the above technical solution, the inner member composed of two guide vanes with relative torsion and inclination can make the bubbles generated in the gas-solid mixed medium break when contacting the inner member. At the same time, since the guide vanes are inclined around the first axis and the second axis at the same time, the guide vane main flow surface has an upward movement trend everywhere, so it is difficult to form an "air cushion" below, thereby preventing the "air cushion" from reducing the effective contact of gas-solid and the overall effective space of the fluidized bed, and improving the reaction efficiency. BRIEF DESCRIPTION OF DRAWINGS

[0021] Figure 1 is a structural schematic diagram of an embodiment of the inner member described in the present application;

[0022] Figure 2 is a structural schematic diagram of another embodiment of the inner member described in the present application;

[0023] Figure 3 is a structural schematic diagram of an embodiment of the fluidized bed reactor described in the present application;

[0024] Figure 4 is a structural schematic diagram of an arrangement of the internal member described in the present application;

[0025] Figure 5 is a structural schematic diagram of an embodiment of the cone member described in the present application;

[0026] Figure 6 is a structural schematic diagram of an arrangement of a plurality of cone member units described in the present application.

[0027] BRIEF DESCRIPTION OF DRAWINGS

[0028] 1 - reactor shell, 2 - reactor cone bottom, 3 - air feed pipe, 4 - air distribution plate, 5 - gas-solid mixing zone, 6 - aromatic / ammonia distributor, 7 - dense phase zone, 8 - heat removal pipe, 9 - internal member, 901 - support, 902 - first guide vane, 903 - through hole, 904 - horizontal support, 905 - second guide vane, 10 - interface influencing zone, 11 - cone member unit, 1101 - cone member, 12 - dilute phase zone, 13 - settler, 14 - cyclone, 15 - outflow line. DETAILED DESCRIPTION

[0029] The specific embodiments of the present application will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are merely intended to illustrate and explain the present application, and should not be used to limit the present application.

[0030] In the present application, the orientation words such as "upper", "lower", "top", "bottom" used without the contrary description generally refer to the orientation of the device or equipment in the use state. It should be noted that this is only for the convenience of describing the present application, and should not be understood as a limitation on the present application.

[0031] In addition, the terms "first", "second", etc. are only for the purpose of description, and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features.

[0032] In the present application, the meaning of "a plurality of" is at least two, for example, two, three, etc., unless otherwise specifically limited.

[0033] In one aspect, the present application provides an inner structure comprising a set of guide vanes, the set of guide vanes comprising a first guide vane 902 and a second guide vane 905, the first guide vane 902 and the second guide vane 905 being oppositely inclined relative to a horizontal plane about a horizontal first axis and oppositely inclined relative to the horizontal plane about a horizontal second axis, the first axis being perpendicular to the second axis, edges of the first guide vane 902 and the second guide vane 905 intersecting at a point.

[0034] The first guide vane 902 and the second guide vane 905 being oppositely inclined relative to a horizontal plane about a horizontal first axis means that the first guide vane 902 and the second guide vane 905 are arranged in opposite directions about the first axis as the rotation axis. Similarly, the first guide vane 902 and the second guide vane 905 being oppositely inclined relative to the horizontal plane about a horizontal second axis means that the first guide vane 902 and the second guide vane 905 are arranged in opposite directions about the second axis. Here, the oppositely should be understood as in opposite directions, which is a relative concept, rather than directly indicating the direction of inclination.

[0035] It should be noted that the fluidized bed reactor described in the present application generally refers to a fluidized bed reaction device (referred to as a fluidized bed for short), which is a reactor that utilizes gas or liquid to pass through a granular solid layer to make the solid particles in a suspended motion state and carry out a gas-solid phase reaction process or a liquid-solid phase reaction process. When the flow rate of the fluid passing through the bed layer gradually increases to a certain value, the particles in the bed layer become loose, the interstitial space between the particles increases, and the volume of the bed layer expands. If the flow rate is further increased, the bed layer will not be able to maintain a fixed state. At this time, the particles are all suspended in the fluid and show a rather irregular motion. With the increase of the flow rate, the motion of the particles becomes more intense, and the expansion of the bed layer also increases, but the particles still remain in the bed layer and are not carried out by the fluid. This state of the bed layer is similar to that of a liquid and is called a fluidized bed.

[0036] Fluidized bed gas refers to the gas that drives the movement of solid particles in the fluidized bed. Generally, the gas flows from bottom to top in the fluidized bed.

[0037] However, there is often a phenomenon of uneven mixing of reaction raw gas and catalyst solid particles in the fluidized bed, which affects the conversion rate of the reaction, reduces the utilization rate of raw materials, and increases the difficulty of product separation. Due to the existence and movement of gas bubbles, backmixing of solid particles and reaction gas phase products in the bed layer will occur. The residence time distribution of gas and solid phases in the fluidized bed is uneven, which will also cause the intensification of side reactions such as over-oxidation and ammonia burning in, for example, aromatic ammoxidation reactions, significantly reducing the conversion rate of the reaction and the selectivity of the target product aryl nitrile.

[0038] The inventor has found through a large number of experiments and observations that the horizontal components usually arranged in the fluidized bed or the components having horizontal parts and small inclination parts usually have some inherent defects, such as, under the horizontal position, "air cushion" appears when the gas velocity of the bed is high, which is an air mass containing a small amount of solid phase, and the "air cushion" reduces the effective contact of the gas-solid and the overall effective space of the fluidized bed.

[0039] It is also found that the vertical components arranged in the fluidized bed can improve the fluidization quality and reduce the unstable fluidization phenomena such as "bubbles", "channeling" and "slugging", but at the same time, the vertical components are consistent with the main direction of the gas-solid flow, and "stagnant layer" is easily formed around the components, which has an adverse effect on the mass and heat transfer.

[0040] The inner component 9 in the present application is composed of the first and second guide vanes 902 and 905 which are relatively twisted and inclined, so that the large bubbles in the gas-solid mixed medium can be broken when contacting the inner component 9. At the same time, since the first and second guide vanes 902 and 905 are inclined around the first and second axes, the small bubbles have an upward movement tendency when contacting the main flow surface of the guide vanes, so that the small bubbles are difficult to gather below and form "air cushion", thereby preventing the "air cushion" from reducing the effective contact of the gas-solid and the overall effective space of the fluidized bed, and improving the reaction efficiency. Due to the special structure, the inner component 9 can overcome the disadvantage that "air cushion" is easily formed below the horizontal inner component, and can avoid the phenomenon that "stagnant layer" is easily formed around the simple vertical component, so as to improve the fluidization quality, reduce the unstable fluidization phenomena such as "bubbles", "channeling" and "slugging", and inhibit the back mixing of particles, improve the residence time distribution of particles in the fluidized bed, and solve the problems of low raw material utilization and many by-products caused by the intensified side reaction. The first and second guide vanes 902 and 905 can break the large bubbles with different flow directions in the bed, and further improve the reaction efficiency in the fluidized bed. The thickness of the first and second guide vanes 902 and 905 can be selected according to the material, fixing method, inclination angle and flow velocity of the gas-solid two-phase medium. As a specific embodiment, the thickness of the guide vanes 902 can be set to 5-50 mm, and preferably 10 mm.

[0041] As a specific embodiment, the inclination angle of the first and second guide vanes 902 and 905 relative to the first axis is 15°-75°, preferably 30-60°, and more preferably 45°; and the inclination angle of the first and second guide vanes 902 and 905 around the second axis is 0°-60°, preferably 30-60°, and more preferably 45°.

[0042] To further prevent the small bubbles formed by breaking the large bubbles from gathering, as shown in Figure 1 In order to avoid the vortex formed by the gas-solid mixture under the blades affecting the fluidization performance, the first guide vane 902 and the second guide vane 905 are provided with through holes 903, small bubbles can directly pass through the through holes 903, and large bubbles can also be broken under the extrusion of the gas-solid two-phase medium and the first guide vane 902 and the second guide vane 905 and the through holes 903, thereby becoming small bubbles, so as to improve the reaction efficiency. Further, the first guide vane 902 and the second guide vane 905 include a plurality of through holes 903, which are arranged in an array on the main flow surface of the first guide vane 902 and the second guide vane 905. The plurality of through holes 903 can further break the large bubbles and more efficiently make the gas-solid two-phase medium flow through the first guide vane 902 and the second guide vane 905, thereby reducing the resistance of the medium flow. The number of through holes on each first guide vane 902 and second guide vane 905 is 3-9. The plurality of through holes can be uniformly distributed on the first guide vane 902 and the second guide vane 905, or arranged in an array, for example, including a plurality of rows of through holes 903 arranged in an array.

[0043] In order to further strengthen the destruction of large bubbles in the bed layer by the inner member 9 and improve the reaction efficiency, as shown in Figure 2 Figure 4 The inner member further includes a vertically arranged support rod 901, and a plurality of guide vane groups are arranged on the support rod 901 in the vertical direction. The first guide vane 902 and the second guide vane 905 of the upper and lower adjacent guide vane groups are oppositely inclined around the second axis. The first axis and the second axis of the upper and lower adjacent guide vane groups are arranged in parallel, so that the relative positions of the two guide vane groups are aligned, and the upper and lower adjacent first guide vanes 902 or second guide vanes 905 are oppositely inclined around the second axis, which can make the gas-solid two-phase medium flow in an "S" shape between the two first guide vanes 902 or second guide vanes 905, which is beneficial to the breaking of large bubbles. The number of layers of guide vane groups can be selected according to the properties of the gas-solid two-phase medium. Too many layers of guide vane groups can cause excessive flow resistance of the medium in the bed layer, so the selection needs to be balanced. Preferably, the guide vane group is provided with 3-5 layers, and more preferably, 3 layers. The width of the support rod 901 is not greater than the width of the guide vane 902, and is preferably 0.4-1.0 times the width of the guide vane.

[0044] The first guide vane 902 and the second guide vane 905 can have various shapes, which can be a structure with the middle part bent downward, or, as shown in​Figure 1 As shown, the first guide vanes 902 and the second guide vanes 905 can also be plate-shaped structures, the vanes being one of trapezoidal, triangular and rectangular, preferably rectangular, as a specific embodiment, the first guide vanes 902 and the second guide vanes 905 can have the same shape to uniformly act on the gas-solid two-phase medium, and the support rod 901 is arranged at the intersection position of the two first guide vanes 902 and the second guide vanes 905, which can be arranged at the center position of the two vanes, so that the inner member 9 is centrally symmetric.

[0045] The second aspect of the present application provides a fluidized bed reactor, which comprises a dilute phase zone 12 and a dense phase zone 7 arranged in sequence along the axial direction of the fluidized bed reactor, and the inner member 9 described in the above technical solution is arranged in the dense phase zone 7. The bubbles in the bed layer have a tendency to grow and coalesce upward along the axial direction of the fluidized bed reactor, and the diameter of the bubbles reaches the maximum at a certain position in the dense phase zone 7, so that the inner member 9 arranged at this position can effectively break the large bubbles into a large number of small bubbles, thereby improving the fluidization quality and the gas-solid contact efficiency and improving the reaction rate.

[0046] The fluidized bed reactor can be as shown in Figure 3 As shown, the reactor shell 1 is provided with a reactor cone bottom 2 at the bottom, a gas-solid mixing zone 5 is arranged at the upper part of the reactor cone 2, an air feeding pipe 3, an air distribution plate 4 and an aromatic hydrocarbon / ammonia distributor 6 are arranged in the gas-solid mixing zone 5 to mix the solid particles with the fluidizing gas and the reaction gas and form a fluidized state in the gas-solid mixing zone 5, a dense phase zone 7 is arranged above the gas-solid mixing zone 5, a heat removal pipe 8 for removing the heat generated in the reaction process is arranged in the dense phase zone 7, the heat removal pipe 8 can be vertically arranged in multiple and connected in sequence, the multiple heat removal pipes 8 can be arranged in the horizontal direction and spaced apart from each other, and the heat removal pipes 8 can be arranged in a square, triangular or ring shape.

[0047] A dilute phase zone 12 is arranged above the dense phase zone 7, the reactor shell 1 is provided with a settler 13 at the dilute phase zone, the top of the reactor shell 1 is provided with an outflow pipe 15, and a cyclone separator 14 is further arranged in the reactor shell 1.

[0048] As a specific embodiment, as shown in Figures 3-4As shown, the fluidized bed reactor further includes multiple heat-removing pipes 8 spaced apart within the dense phase zone 7, and multiple internal components 9 disposed within the intervals of the heat-removing pipes 8. Furthermore, the internal components 9 can be positioned at the center of the interval between two adjacent heat-removing pipes 8. To further improve the effect of breaking up bubbles and inhibiting bubble growth, the height of the internal component 9 can be set to 1.0-6.0 times the diameter of the reactor shell, preferably 2.0-4.0 times. The span (distance between the farthest points) between the first guide vane 902 and the second guide vane 905 of the internal component 9 can be set to 0.05-0.45 times the interval distance between adjacent heat-removing pipes 8 on both sides, and the width of the first guide vane 902 and the second guide vane 905 can be set to 0.4-1.0 times the diameter of the heat-removing pipe 8. The spacing between two adjacent upper and lower guide vane groups can be set to 2-20 times the spacing between the heat-removing pipes 8.

[0049] To further enhance the stability of the internal component 9, such as Figure 2 As shown, the fluidized bed reactor also includes a horizontal support 904 connected between the internal component 9 and the heat removal pipe 8.

[0050] To mitigate end effects such as particle entrainment and bed surface oscillation caused by bubble overflow in the interface influence zone 10, as well as backmixing, the fluidized bed reactor further includes an interface influence zone 10 located between the dilute phase zone 12 and the dense phase zone 7, and a conical component 1101 disposed within the interface influence zone 10, with the tip of the conical component 1101 facing downwards. The conical component 1101 can be a solid or hollow conical structure, such as a cone or a polygonal pyramid. Since open hollow structures easily create dead zones, making it difficult to utilize materials, it is preferable that the conical component 1101 is a solid structure. To reduce weight and lower the load on the supporting structure, the conical component 1101 is more preferably a hollow closed structure. Taking a cone as an example, the height-to-diameter ratio of the conical component 1101 can be set to 0.3-3.

[0051] To further enhance the effect on the overflowing bubbles, such as Figure 6 As shown, multiple conical components 1101 are arranged in an array along the horizontal direction to form a conical component unit 11. The array arrangement can be a square array, a triangular array, or a circular array, with a circular array being preferred.

[0052] Furthermore, the fluidized bed reactor includes a plurality of vertically spaced conical component units 11. Two adjacent conical component units 11 can be aligned or staggered, and the spacing between adjacent layers of conical component units 11 can be set to 0.05-0.3 times the diameter of the fluidized bed reactor. The number of conical component units 11 can be set to 2-3 layers.

[0053] In order to further illustrate the advantages of the scheme of the present application, several preferred embodiments of the present application are presented below as examples:

[0054]

Example 1

[0055] The fluidized bed reactor is used for aromatic aminooxidation reaction. The reaction raw materials of meta-xylene, ammonia and air are subjected to gas phase aminooxidation reaction under the action of a catalyst. The molar ratio of meta-xylene, ammonia and air is 1:7:36. The reaction temperature is 425℃. The reaction pressure is 0.02Mpa. The apparent gas velocity of the reactor is 0.4m / s. The target product aryl nitrile (m-xylylene cyanide) is obtained.

[0056] The parameters of the inner member 9 are set as follows: the inclination angle of the first guide vane 902 and the second guide vane 905 to the first axis is set to 15°, the inclination angle to the second axis is set to 0°, the horizontal span between the first guide vane 902 and the second guide vane 905 is set to 0.15 times the distance between adjacent heat removal pipes 8, the width of the first guide vane 902 and the second guide vane 905 is set to 0.4 times the diameter of the heat removal pipe, the thickness of the first guide vane 902 and the second guide vane 905 is set to 10mm, only one layer of guide vane group is set, and 3 through holes 903 are set on each guide vane.

[0057] It is measured that the bed expansion coefficient (the ratio of the bed height during normal fluidization to the static bed height) is 1.42; the maximum values of the standard deviation of pressure fluctuation in the dense phase reaction zone and the interface influence zone are 521Pa and 119Pa respectively; the yield of the target product aryl nitrile is 77.5%; it is illustrated that the device can promote the improvement of the bed fluidization quality and the increase of the product yield.

[0058]

Example 2

[0059] The parameters of the inner member 9 are basically the same as those in Example 1, except that the inclination angle of the first guide vane 902 and the second guide vane 905 on each member unit around the second axis is 45° and is centrally symmetric.

[0060] It is measured that the bed expansion coefficient is 1.42; the maximum values of the standard deviation of pressure fluctuation in the dense phase reaction zone and the interface influence zone are 503Pa and 111Pa respectively; the yield of the target product aryl nitrile is 77.6%.

[0061]

Example 3

[0062] The parameters of the inner member 9 are basically consistent with those of Embodiment 2, except that the inclination angle of the first guide vane 902 and the second guide vane 905 on each member unit around the second axis is 30°, the horizontal span between the first guide vane 902 and the second guide vane 905 is 0.3 times the distance between adjacent heat removal pipes 8, and the single-piece guide vane is provided with 8 through holes 903.

[0063] It is measured that the bed expansion coefficient is 1.42, the maximum standard deviation of pressure pulsation in the dense phase reaction zone and the interface influence zone is 497 Pa and 106 Pa respectively, and the yield of the target product aryl nitrile is 79.3%.

[0064]

Embodiment 4

[0065] The parameters of the inner member 9 are basically consistent with those of Embodiment 3, except that the inner member 9 is provided with 3 layers of guide vane groups, and the distance between the upper and lower adjacent guide vane groups is 5 times the distance between adjacent heat removal pipes 8.

[0066] It is measured that the bed expansion coefficient is 1.43, the maximum standard deviation of pressure pulsation in the dense phase reaction zone and the interface influence zone is 473 Pa and 103 Pa respectively, and the yield of the target product aryl nitrile is 80.6%.

[0067]

Embodiment 5

[0068] The parameters of the inner member 9 are basically consistent with those of Embodiment 4, and further, the interface influence zone is provided with a cone member unit 11, the height-diameter ratio of a single cone member 1101 is 1.5, and the cone member unit 11 is provided with 2 layers, and the distance between the adjacent two layers of cone member units 11 is 0.1 times the diameter of the fluidized bed reactor.

[0069] It is measured that the bed expansion coefficient is 1.5, the maximum standard deviation of pressure pulsation in the dense phase reaction zone and the interface influence zone is 442 Pa and 51 Pa respectively, and the yield of the target product aryl nitrile is 82.0%.

[0070] In order to reflect the advantages of the technical scheme, a reaction of a fluidized bed reactor without the inner member 9 and the cone member unit 11 is also proposed as a comparative example:

[0071]

Comparative Example 1

[0072] The fluidized bed reactor is used for the oxidation reaction of aromatic hydrocarbons, and the m-xylene, ammonia and air react with each other in the gas phase under the action of a catalyst, the molar ratio of m-xylene, ammonia and air is 1:7:36, the reaction temperature is 425℃, the reaction pressure is 0.02Mpa, and the superficial gas velocity of the reactor is 0.4m / s, so as to obtain the target product aryl nitrile. (The reaction conditions are consistent with those of Embodiment 1, but the inner member 9 and the cone member unit 11 described in the application are not provided.)

[0073] The measured results are as follows: bed expansion coefficient 1.32; maximum standard deviation of pressure fluctuation of dense phase reaction zone and interface influence zone are 625 Pa and 155 Pa respectively; yield of target product aryl cyanide 74.9%.

[0074] The preferred embodiments of the present application are described in detail above with reference to the drawings, but the present application is not limited thereto. Within the technical concept of the present application, various simple modifications can be made to the technical solutions of the present application, including the combination of various specific technical features in any suitable manner. In order to avoid unnecessary repetition, the present application does not further describe various possible combination manners. However, these simple modifications and combinations should also be regarded as the disclosed content of the present application and belong to the protection scope of the present application.

Claims

1. A fluidized bed reactor, characterized by, The fluidized bed reactor comprises a dilute phase zone (12) and a dense phase zone (7) arranged in sequence along the axial direction of the fluidized bed reactor, the dense phase zone (7) is provided with an internal component (9), the internal component (9) comprises a guide vane group, the guide vane group comprises a first guide vane (902) and a second guide vane (905), the first guide vane (902) and the second guide vane (905) are oppositely inclined relative to the horizontal plane around a horizontal first axis and oppositely inclined relative to the horizontal plane around a horizontal second axis, the first axis is perpendicular to the second axis, the edges of the first guide vane (902) and the second guide vane (905) intersect at a point, and the first guide vane (902) and the second guide vane (905) are provided with through holes (903); The internal component (9) further comprises a vertically arranged support rod (901), a plurality of layers of the guide vane group are arranged in the vertical direction on the support rod (901), the first guide vane (902) and the second guide vane (905) of the upper and lower two adjacent guide vane groups are oppositely inclined around the second axis; The fluidized bed reactor further comprises a heat removal pipe (8) and a horizontal support (904), a plurality of heat removal pipes (8) are arranged in the dense phase zone (7), a plurality of internal components (9) are arranged in the space between the heat removal pipes (8), and the horizontal support (904) is connected between the internal components (9) and the heat removal pipes (8); The fluidized bed reactor further comprises an interface influencing zone (10) between the dilute phase zone (12) and the dense phase zone (7) and a cone component (1101) arranged in the interface influencing zone (10), and the tip of the cone component (1101) faces downward.

2. The fluidized bed reactor of claim 1, wherein, The inclination angle of the first guide vane (902) and the second guide vane (905) relative to the first axis is 15°-75°; and / or, the inclination angle of the first guide vane (902) and the second guide vane (905) around the second axis is 30°-60°.

3. The fluidized bed reactor of claim 1, wherein, The first guide vane (902) and the second guide vane (905) comprise a plurality of through holes (903), and the through holes (903) are arranged in an array on the main flow surface of the first guide vane (902) and the second guide vane (905).

4. Fluidized bed reactor according to any one of claims 1 to 3, characterized in that The first guide vane (902) and the second guide vane (905) are plate-shaped structures, the vane is one of trapezoidal, triangular and rectangular, and / or the first guide vane (902) and the second guide vane (905) have the same shape.

5. The fluidized bed reactor of claim 1, wherein, A plurality of cone components (1101) are arranged in an array in the horizontal direction and form a cone component unit (11), and the fluidized bed reactor comprises a plurality of vertically spaced cone component units (11).

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