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CN-121988237-A - Fluidized bed reactor and application thereof

CN121988237ACN 121988237 ACN121988237 ACN 121988237ACN-121988237-A

Abstract

The present invention relates to a fluidized bed reactor and its use. The fluidized bed reactor comprises an inner cavity and a flow guide assembly arranged in the inner cavity, wherein the flow guide assembly comprises a plurality of connecting rods which are arranged side by side, the sum of the angle values of the left included angle of one connecting rod and the left included angle of the other connecting rod is more than or equal to 90 degrees, and the sum of the angle values of the right included angle of one connecting rod and the right included angle of the other connecting rod is more than or equal to 90 degrees. According to the invention, the contact and mixing of the gas and the solid can be more effectively promoted, and the gas-solid fluidization quality is further improved.

Inventors

  • XU JUN
  • QI GUOZHEN
  • YE JUNXIANG
  • LIU ZIYAN

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
20241108

Claims (12)

  1. 1. A fluidized bed reactor comprising an inner cavity and a flow guiding assembly disposed in the inner cavity, wherein The flow guide assembly comprises a plurality of (e.g. 4-50, preferably 9-39) connecting rods arranged side by side, the central axes of which are oriented substantially parallel and in substantially the same horizontal plane in the inner chamber, At least one upright post is vertically arranged on each connecting rod, an elongated guide vane (respectively called a left elongated guide vane and a right elongated guide vane) is respectively arranged on each upright post in a mode of respectively extending towards the left side and the right side of the connecting rod by taking the central axis direction of the connecting rod as a symmetrical axis, On each connecting rod, the projection of the length direction of the left-direction long guide vane on the horizontal plane forms an included angle (called a left-direction included angle) with the central axis direction of the connecting rod, the projection of the length direction of the right-direction long guide vane on the horizontal plane forms an included angle (called a right-direction included angle) with the central axis direction of the connecting rod, And selecting any two adjacent connecting rods from the flow guiding assembly, wherein the sum of the angle values of the left included angle of one connecting rod and the left included angle of the other connecting rod is more than or equal to 90 degrees (preferably 90-180 degrees), and the sum of the angle values of the right included angle of one connecting rod and the right included angle of the other connecting rod is more than or equal to 90 degrees (preferably 90-180 degrees).
  2. 2. The fluidized bed reactor of claim 1, wherein in any two of the adjacent connecting rods, the left or right included angle of the one connecting rod has a value of 45 ° to 90 °, and the left or right included angle of the other connecting rod has a value of 45 ° to 90 °.
  3. 3. The fluidized bed reactor of claim 1, wherein the elongated baffles have an angle of 30-90 ° (preferably 60-90 °) with the central axis of the column in the length direction.
  4. 4. The fluidized bed reactor of claim 1, wherein the height direction of the elongated guide vane is at an angle of 0 to 30 ° (preferably 0 to 10 °) or 0 to-30 ° (preferably 0 to-10 °) to the central axis direction of the upright.
  5. 5. The fluidized bed reactor of claim 1, wherein the elongated baffle has a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end, the elongated baffle and the upright being connected to each other at the proximal end, a first cross-section and a second cross-section being obtained when the elongated body is cut at any two positions along a height direction of the elongated baffle, respectively, wherein the first cross-section is closer to the proximal end than the second cross-section, an area of the first cross-section is provided as A1 (in mm 2 ), an area of the second cross-section is provided as A2 (in mm 2 ), a1≥a2 (preferably A1> A2).
  6. 6. The fluidized bed reactor of claim 1, wherein the elongate baffle has a proximal end and a distal end, and An elongate body extending between the proximal end and the distal end, the proximal end having a cross-sectional area An (in mm 2 ) and the distal end having a cross-sectional area Af (in mm 2 ), an/Af = 1-25000 (preferably 1.2-15).
  7. 7. A fluidized bed reactor as set forth in claim 1 wherein on each of said connecting rods, the spacing (based on the central axis) between adjacent two of said columns is 100-1000mm (preferably 200-400 mm).
  8. 8. A fluidized bed reactor according to claim 1 wherein the minimum horizontal distance Dm between the left elongate deflector of one connecting rod and the right elongate deflector of the other connecting rod (on the side closer to the left elongate deflector) is greater than or equal to 50mm (preferably 120-400 mm) when looking at any two adjacent connecting rods.
  9. 9. A fluidized bed reactor as set forth in claim 1 wherein said flow directing elements are arranged in multiple layers (e.g., 2-20 layers) along the central axis of said inner chamber, the vertical spacing between the layers (based on the central axis of the connecting rod) being 0.1-0.3 times (preferably 0.12-0.25 times) the diameter of said inner chamber.
  10. 10. The fluidized bed reactor of claim 9, further comprising a gas distributor disposed at a bottom of the inner chamber, wherein a flow guide member at a lowermost layer along a central axis direction of the inner chamber is disposed above the gas distributor and has a vertical distance (based on a central axis of a connecting rod) from 0.1 to 0.2 times (preferably 0.12 to 0.2 times) a diameter of the inner chamber.
  11. 11. The fluidized bed reactor as set forth in claim 1, wherein on each of said connecting rods, an angle a between a height direction of the left-hand elongated guide vane and a central axis of said column is set, and an angle B between a height direction of the right-hand elongated guide vane and a central axis of said column is set, and a = B.
  12. 12. A fluidized bed reaction process comprising the step of performing a chemical reaction in the fluidized bed reactor of any one of claims 1 to 11.

Description

Fluidized bed reactor and application thereof Technical Field The invention relates to the technical field of solid fluidization. More particularly, the present invention relates to a fluidized bed reactor and its use. Background Fluidized bed reactors refer to devices in which a gas undergoes a chemical reaction in a bubbling bed of solid material or catalyst, also known as "bubbling bed reactors". The gas will, over a range of flow rates, vigorously agitate the solid particles of catalyst or material packed to a certain thickness (bed) to resemble a boiling liquid and have some properties of the liquid, such as fluid pressure against the walls, overflow and viscosity. Compared with a fixed bed reactor, the fluidized bed reactor can realize continuous input and output of solid materials, has good heat transfer performance due to movement of fluid and particles, has uniform temperature inside the bed layer, is easy to control, is particularly suitable for strong exothermic reaction, is convenient for continuous regeneration and circulation operation of the catalyst, and is suitable for the process with high catalyst deactivation rate. The fluidized bed is a gas-solid two-phase reaction process method commonly used in industry, the reaction performance of the process is closely related to the fluidization quality of particles in the bed, and bubbles are generated in the gas-solid two phases due to the fluidization characteristic of part of the particles, so that the residence time of the particles in the reactor is unevenly distributed, the bed frequently fluctuates, and the production efficiency is greatly reduced. To solve the above-mentioned drawbacks, a method of adding a foam breaking member to the inside of a reactor is often employed. The fluidized bed has the functions of breaking bubbles and limiting bubble growth, so that the residence time of gas in the bed is homogeneous, the gas exchange amount between bubble phase and emulsion phase is increased, the gas-solid contact efficiency is raised, the chemical reaction conversion rate is raised, and the selectivity and yield are raised. Therefore, research and improvement of components have become an important way for improving the production strength of the fluidized bed reactor and strengthening the fluidization process. The bubble breaking inner member of the fluidized bed reactor in the prior art mainly comprises three types of horizontal members, vertical members and composite members. The horizontal members are classified into porous baffles (screens), louver baffles (also called guide baffles or inclined-piece baffles), corrugated baffles, and the like. The horizontal member divides the bed into several sections in series, redistributes the gas, reduces the bubble size, and improves the mass and heat transfer between the gas and solid. Porous baffles are most commonly found in horizontal members and are similar in structure to porous distribution plates, but have a relatively high open cell content, typically 10% -40%, with the cell diameter and baffle spacing typically determined empirically. The aperture ratio of the porous baffle plate also has an extremely high phenomenon, namely a screen. The particles can move up and down through the holes, the pressure difference between the upper and lower plates is small, and the mechanical property of the material is not high. Below the porous barrier there is typically a dilute phase zone of a certain thickness, also known as an air cushion zone, where the particle concentration is low, inhibiting particle back mixing. The porous baffle can effectively limit the growth of bubbles and the back mixing of particles and gas, and is suitable for occasions with higher conversion rate requirements in solid phase processing. At present, research on a porous baffle is mainly focused on the influence research of the porous baffle on the classification of particles and the gas-solid flow characteristics in a bubbling fluidized bed, and the porous baffle with small opening diameters and narrow baffle intervals is found to improve the particle classification efficiency, reduce the residence time of small particles and prolong the residence time of large particles. The single-rotation guide baffle is another horizontal member with more application, and the related research is carried out on the influence of the conversion rate and selectivity of the single-rotation guide baffle in the production process and the influence of baffle structural parameters on the gas-solid flow characteristics in the bed, so that the smaller blade spacing and blade inclination angle can obviously enhance the inhibition effect of the single-rotation guide baffle on the gas-phase axial back mixing, and the single-rotation guide baffle is successfully applied to the production processes of benzene oxidation maleic anhydride, naphthalene oxidation phthalic anhydride, butene oxidative dehydrogenation and the like at present The vertical int