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CN-121988232-A - Annular tubular distributor, fluidized bed reaction device, gas phase reaction method and application

CN121988232ACN 121988232 ACN121988232 ACN 121988232ACN-121988232-A

Abstract

The invention relates to the technical field of feeding structures, and discloses a ring-shaped tubular distributor, a fluidized bed reaction device, a gas phase reaction method and application, wherein the ring-shaped tubular distributor comprises a plurality of ring pipes which are concentrically arranged from inside to outside, and each ring pipe is provided with a nozzle; the device comprises a plurality of annular pipes, a plurality of connecting pipes, a plurality of tangential feeding pipes, a plurality of discharging pipes, a plurality of connecting pipes and a plurality of connecting pipes, wherein the adjacent two annular pipes are communicated through the plurality of connecting pipes which are arranged at intervals along the circumferential direction, the discharging end of each connecting pipe is connected with the tangential direction of the annular pipe of the inner layer, the tangential direction of the annular pipe of the outermost layer extends to form the tangential feeding pipes, and the tangential feeding pipes are provided with the plurality of tangential feeding pipes which are arranged at intervals along the circumferential direction. The invention can be adapted to industrial large reactors without reducing the production efficiency.

Inventors

  • YE JUNXIANG
  • XU JUN
  • LI YONGZHENG
  • ZHONG SIQING

Assignees

  • 中国石油化工股份有限公司
  • 中石化（上海）石油化工研究院有限公司

Dates

Publication Date
20260508
Application Date
20241107

Claims (10)

  1. 1. A ring-type tubular distributor, characterized in that the ring-type tubular distributor (4) comprises a plurality of annular tubes (13) concentrically arranged from inside to outside, each annular tube (13) being provided with a nozzle (16); Wherein two adjacent ring pipes (13) are communicated through a plurality of connecting pipes (14) which are arranged at intervals along the circumferential direction, and the discharge end of each connecting pipe (14) is connected with the tangential direction of the ring pipe (13) of the inner layer; Among the plurality of annular pipes (13), a tangential feed pipe (15) is formed by tangential extension of the annular pipe (13) on the outermost layer, and the tangential feed pipe (15) is provided with a plurality of tangential feed pipes (15) which are circumferentially arranged at intervals.
  2. 2. A loop-type pipe distributor according to claim 1, characterized in that the pipe diameters of two adjacent loops (13) are the same, or The plurality of annular pipes (13) are sequentially divided into a1 st annular pipe part outwards along the center of the annular pipe type distributor, an N th annular pipe part, wherein N is more than or equal to 2, and the pipe diameter of the annular pipe (13) in the N-1 th annular pipe part is smaller than the pipe diameter of the annular pipe (13) in the N th annular pipe part; preferably the number of loops in each loop portion is 1 or more, and/or Preferably the same pipe diameter of the same pipe section, and/or Preferably the number of loops in each loop portion is the same, or When the number of the annular pipes in the annular pipe parts is different, the number of the annular pipes in the N-th annular pipe part is more than or equal to the number of the annular pipes in the N-1-th annular pipe part.
  3. 3. The loop-type pipe distributor according to claim 1 or 2, characterized in that the ratio of the pipe diameter of the loop (13) in the N-1 th loop section to the pipe diameter of the loop (13) in the N-th loop section is 0.3-1, preferably 0.3-0.8.
  4. 4. A loop-type pipe distributor according to any of claims 1-3, characterized in that the ratio of the cross-sectional flow area of the feed end to the cross-sectional flow area of the discharge end of the adapter pipe (14) is 0.5-2, preferably 1-1.9, and/or In the two adjacent annular pipes (13), the included angle alpha between the flow direction of the connecting part of the annular pipe (13) of the outer layer and the connecting pipe (14) and the flow direction of the connecting pipe (14) is 0-180 degrees, preferably 90-170 degrees.
  5. 5. The loop-type pipe distributor according to any one of claims 1-4, wherein the loop (13) is arranged horizontally, the nozzles (16) on the loop (13) are arranged vertically downwards, and/or The diameter of the nozzle (16) on the annular pipe (13) positioned in the N-1 annular pipe part is smaller than or equal to the diameter of the nozzle (16) on the annular pipe (13) positioned in the N annular pipe part; preferably, the ratio of the diameter of the nozzle (16) on the loop (13) located in the N-1 th loop portion to the diameter of the nozzle (16) on the loop (13) located in the N-th loop portion is 0.35 to 0.9.
  6. 6. A fluidized bed reaction apparatus, characterized in that it employs a loop-type pipe distributor (4) according to any one of claims 1 to 5.
  7. 7. The fluidized bed reactor according to claim 6, wherein a plurality of annular tube distributors (4) are provided, a plurality of the annular tube distributors being arranged at intervals in the axial height direction in the fluidized bed reaction chamber, and/or The reaction cavity of the fluidized bed reaction device comprises a cylindrical section and a conical section with a large upper part and a small lower part, wherein the bottom of the cylindrical section is connected with the large end of the conical section, and the ratio of the vertical distance between the annular tubular distributor and the bottom of the cylindrical section to the height of the reaction cavity is 0.01-0.1.
  8. 8. A gas phase reaction method, characterized in that it employs the fluidized bed reaction apparatus according to claim 6 or 7.
  9. 9. The gas phase reaction method according to claim 8, wherein the superficial linear velocity of the gas in the fluidized bed reaction apparatus is 0.1 to 0.8m/s, and/or The non-uniformity M of the nozzle jet flow of the annular tube type distributor is 0-0.35, wherein the non-uniformity calculating method comprises the following steps of Wherein n is the number of nozzles, u i is the nozzle ejection flow, Is the average flow rate of the spray nozzle.
  10. 10. Use of a loop-type tubular distributor according to any one of claims 1 to 5, a fluidized bed reaction apparatus according to claim 6 or 7 or a gas phase reaction process according to claim 8 or 9 for the preparation of nitriles by hydrogenation or hydrocarbon ammoxidation; the method is preferably applied to the preparation of isophthalonitrile by the cold hydrogenation reaction of silicon tetrachloride or the ammoxidation of m-xylene; more preferably, the reaction temperature for preparing isophthalonitrile by ammoxidation of metaxylene is 300-500 ℃.

Description

Annular tubular distributor, fluidized bed reaction device, gas phase reaction method and application Technical Field The invention relates to the technical field of feeding structures, in particular to a ring-type tubular distributor, a fluidized bed reaction device, a gas phase reaction method and application. Background A loop-type pipe distributor is a commonly used pipe gas distributor, typically consisting of a multi-layer loop with nozzles arranged on the loop to uniformly fill the reactor flow cross section. The annular tubular distributor has the characteristics of no need of bearing the particle lifting function of the plate-type distributor, low structural strength requirement, low manufacturing difficulty and low cost, is suitable for gas feeding distribution of industrial large-scale reactors, but in practical application, the gas uniform distribution effect is deteriorated along with the enlargement of the size of the reactors, and the reaction conversion rate or the product yield is reduced. Disclosure of Invention The invention aims to solve the problems that the gas uniform distribution effect is deteriorated and the reaction conversion rate or the product yield is reduced along with the enlargement of the size of a reactor in the prior art, and provides a ring-type tubular distributor, a fluidized bed reaction device, a gas phase reaction method and application, which can adapt to an industrial large-scale reactor without reducing the production efficiency. In order to achieve the above object, in one aspect, the present invention provides a loop-type pipe distributor including a plurality of loops concentrically arranged from inside to outside, each of the loops being provided with a nozzle thereon; the two adjacent annular pipes are communicated through a plurality of connecting pipes which are arranged at intervals along the circumferential direction, and the discharge end of each connecting pipe is connected with the tangential direction of the annular pipe at the inner layer; Among the annular pipes, the tangential extension of the annular pipe on the outermost layer is provided with tangential feed pipes, and the tangential feed pipes are provided with a plurality of tangential feed pipes and are circumferentially arranged at intervals. In a second aspect, the invention provides a fluidized bed reaction apparatus employing a loop-type tubular distributor according to the invention. In a third aspect, the present invention provides a gas phase reaction process employing a fluidised bed reactor according to the present invention. The annular tube type distributor, the fluidized bed reaction device or the gas phase reaction method are applied to hydrogenation or hydrocarbon ammoxidation to prepare nitriles, preferably to cold hydrogenation of silicon tetrachloride or m-xylene ammoxidation to prepare m-phthalonitrile, and more preferably to the reaction temperature of 300-500 ℃ for m-xylene ammoxidation to prepare m-phthalonitrile. According to the technical scheme, the tangential feed pipes are arranged in the circumferential direction of the outermost annular pipe, the discharge end of each connecting pipe between two adjacent annular pipes is connected in the tangential direction of the circumferential direction of the inner annular pipe, so that the uniformity of material distribution can be enhanced, the annular pipe type distributor can improve the utilization rate of raw materials when applied to the reactor, is suitable for the reactors with different specifications, and can avoid the problem of uneven internal flow fields caused by bias flow even if the reactor is enlarged. Drawings FIG. 1 is a schematic view showing the structure of a fluidized bed reaction apparatus according to an embodiment of the present invention; FIG. 2 is a schematic view showing the structure of a fluidized bed reaction apparatus according to another embodiment of the present invention; FIG. 3 is a schematic view of the structure of a loop-type pipe distributor according to one embodiment of the present invention; FIG. 4 is a schematic view of a ring-type tube distributor according to another embodiment of the present invention; FIG. 5 is an enlarged partial schematic view of FIG. 3; FIG. 6 is an enlarged partial schematic view of FIG. 4; FIG. 7 is a schematic illustration of the connection of the nozzle to the collar of FIG. 3 or FIG. 4; FIG. 8 is a schematic diagram of a prior art loop-type tubular distributor; fig. 9 is a schematic view of a prior art loop-type tube distributor. Description of the reference numerals 1 Gas collecting chamber, 2 fluidized bed reactor, 3 heat exchanger, 4 annular pipe distributor, 5 first material gas feeding pipe, 6 second material gas feeding pipe, 7 gas distributor, 8 third material gas feeding pipe, 10 cyclone separator, 11 effluent pipeline, 12 particle feeding pipe, 13 annular pipe, 14 connecting pipe, 15 tangential feeding pipe and 16 nozzle. Detailed Description