Flow guiding member, fluidized bed reactor, and reaction method

Abstract

The present invention relates to a flow guiding member, a fluidized bed reactor, and a reaction method. The flow guiding member of the present invention comprises an elongated member, wherein the elongated member has a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end, wherein the elongated body comprises at least such a section: when the elongated body is cut at any position in a flow guiding direction within the section, only one pair of farthest-apart points, respectively referred to as a first point and a second point, can be found on the outer periphery of the obtained cross section. The outer periphery of the overall cross section is divided by the first point and the second point into a first line and a second line connected end to end. A straight line segment connecting the first point and the second point is referred to as a dividing line, wherein the length of the first line is set to be L1, the length of the second line is set to be L2, and the ratio of L1 / L2 is greater than 1. In the present invention, a stronger vortex can be formed at the flow guiding member, thereby more effectively promoting gas and solid contact and mixing, and further improving gas-solid fluidization quality.

Description

A flow guiding component, a fluidized bed reactor, and a reaction method. Technical Field

[0001] This invention relates to the field of solid fluidization technology. More specifically, this invention relates to a flow guiding component, a fluidized bed reactor, and a reaction method. Background Technology

[0002] A fluidized bed reactor is a device in which a chemical reaction takes place within a boiling bed composed of solid materials or catalysts; it is also known as a "boiling bed reactor." Within a certain flow rate range, the gas intensely agitates a layer of catalyst or fine solid particles of material of a certain thickness (bed), causing it to behave like a boiling liquid and exhibit some of its properties, such as exerting fluid pressure on the vessel walls, overflow, and viscosity. Compared to fixed bed reactors, fluidized bed reactors allow for continuous input and output of solid materials; the movement of fluids and particles provides excellent heat transfer performance within the bed, resulting in a uniform and easily controllable internal temperature, making them particularly suitable for strongly exothermic reactions; they also facilitate continuous catalyst regeneration and recycling, making them suitable for processes with high catalyst deactivation rates.

[0003] Fluidized beds are typical reactors commonly used in industrial gas-solid two-phase reaction processes. However, due to the fluidization characteristics of some particles, bubbles are generated in the gas-solid two-phase system, resulting in uneven residence time distribution of particles in the reactor and frequent bed fluctuations, thus significantly reducing the yield of the target product. To improve the process, bubble-breaking internal components are generally added inside the reactor. Existing bubble-breaking internal components in fluidized bed reactors mainly fall into three types: horizontal components, vertical components, and composite components. Horizontal components break large bubbles into strip-shaped bubbles after gas passes through them, but these bubbles tend to coalesce again after a certain distance. Vertical components, while simple in structure, only restrict bubble growth and have very limited effect on breaking up bubbles. Composite components, due to their overly complex structure, have limited application in fluidized bed reactors.

[0004] Patent WO2020078414A1 discloses a fluidized bed reactor employing a double trapezoidal component. This double trapezoidal component consists of two sets of perforated baffles with trapezoidal side cross-sections. The long sides of each baffle set are parallel to each other but at different distances, forming a specific angle on the side. The trapezoidal areas enclosed by every two sets of baffles are inverted and overlapped to form a double trapezoidal component unit. These component units are arranged in multiple rows and layers to form a bubble-breaking and flow-guiding component in the dense phase zone of the fluidized bed reactor. Through the multi-layered double trapezoidal baffles with specific angle designs and the flow-guiding hole structure on the baffles, effective breaking of large bubbles in the dense phase bed is achieved, while preventing particle accumulation and blockage on the baffles, thus improving the fluidization quality and reaction efficiency of the particles in the bed. Summary of the Invention

[0005] The inventors of this invention have discovered that although the known solutions in the prior art take into account the breaking of bubbles and the prevention of aggregation during the reaction process, the overall grid-type internal component design is still a traditional bubble-breaking configuration. The local vortex effect is not obvious, making it difficult to achieve radial gas-solid transfer. Under certain process requirements for rising gas velocity, it is difficult to form strong vortices and turbulence, and it is difficult to guarantee the fluidization quality and gas-solid heat and mass transfer efficiency.

[0006] The purpose of this invention is to provide a flow guiding component that can generate stronger vortices in a reactor, thereby more effectively promoting gas-solid contact and mixing, and thus improving the quality of gas-solid fluidization.

[0007] According to a first aspect of the invention, there is a flow guiding member comprising an elongated member having a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end, wherein the elongated body comprises at least a section in which, when the elongated body is cut at any position along the flow guiding direction within the section, only a pair of points furthest apart can be found on the outer periphery of the obtained cross-section (referred to as the total cross-section), referred to as a first point and a second point, respectively, the outer periphery of the total cross-section being divided by the first point and the second point into a first line and a second line connected end to end, the straight line segment connecting the first point and the second point being referred to as a dividing line, and assuming the length of the first line is L1 and the length of the second line is L2, then the value of L1 / L2 is greater than 1.

[0008] According to a second aspect of the invention, there is a fluidized bed reactor comprising a shell and a flow guiding member disposed within the shell, wherein the flow guiding member includes the flow guiding member of the present invention.

[0009] According to a third aspect of the invention, there is a fluidized bed reaction method comprising a step of carrying out a chemical reaction in the fluidized bed reactor of the invention.

[0010] Technical effect

[0011] 1) Through the structural design of the elongated component, the velocity of the airflow flowing through the first surface corresponding to the first line will be greater than the velocity of the airflow flowing through the second surface corresponding to the second line. The velocity difference can form a pressure gradient between the first and second surfaces. Based on this, the high-pressure airflow on the second surface can roll and flow along the spanwise fins to the lower pressure first surface. Combined with the mainstream direction of the fluid, a strong vortex can be formed. This strong vortex can enhance the radial transfer of gas and solid, improve the gas-solid fluidization quality and gas-solid transfer efficiency in the fluidized bed, and thus improve the reaction efficiency.

[0012] 2) When the present invention adopts a combination of elongated and sheet-like components, the radial and axial vortices formed when the airflow from bottom to top flows through the guide component can meet and be further mixed and enhanced, that is, the radial and axial transmission of gas and solid is realized. Compared with using only elongated components, the combination of elongated and sheet-like components has a synergistic effect. The strong vortex obtained by the combined action of the two makes the gas-solid contact and mixing effect better.

[0013] 3) When the present invention adopts a semi-elliptical sheet-like component design, its windward end is an arc similar to the shape of a blade. While the axial fins generate axial vortices, the arc of the blade shape has a better effect on breaking and cutting bubbles.

[0014] 4) The columnar component and connecting rod of the flow guiding component of the present invention can be manufactured by integral molding; the elongated component and the sheet component can be integrally molded with the columnar component, or they can be installed on the columnar component by plug-in fixing according to the needs of the site. The structure is simple and the installation is convenient.

[0015] 5) In the fluidized bed reactor of the present invention, the flow guiding components can be arranged in layers, with multiple evenly spaced connecting rods in each layer, and multiple flow guiding components evenly spaced on each connecting rod; the horizontal projections of the elongated components on opposite sides of adjacent connecting rods are substantially parallel; the included angle formed by the central axes of the connecting rods in each layer can be 90 degrees. This arrangement allows for the generation of radial and axial vortices in different directions in localized areas of each layer. Within a larger reactor space, this further enhances the radial and axial transfer of gas and solid components in different directions, resulting in a stronger vortex mixing effect. Attached Figure Description

[0016] Figure 1 is a first three-dimensional structural schematic diagram of the flow guiding component of the present invention.

[0017] Figure 2 is a schematic diagram of the second three-dimensional structure of the flow guiding component of the present invention.

[0018] Figure 3 is a schematic diagram of the front view of the flow guiding component of the present invention.

[0019] Figure 4 is a side view of the flow guiding component of the present invention.

[0020] Figure 5 is a top view of the flow guiding component of the present invention.

[0021] Figure 6 is a schematic diagram of the cross-sectional structure of the elongated body of the present invention.

[0022] Figure 7 is a schematic diagram of the multi-layer arrangement of the combined finned components of the present invention in a fluidized bed reactor.

[0023] Figure 8 is a three-dimensional schematic diagram of one of the layers in Figure 7.

[0024] Figure 9 is a top view of one of the floors in Figure 7.

[0025] Figure 10 is a schematic diagram of the surface flow field structure of the elongated component of the present invention.

[0026] Explanation of key figure labels:

[0027] 1-Flow guiding component; 10-Columnar component; 11-Elongated component; 111-First surface; 112-Second surface; 113-Proximal end; 114-Distal end; 115-Elongated body; 12-Sheet-shaped component; 13-Connecting rod;

[0028] 2-Elongated body cross-section (total cross-section), 201-First point, 202-Second point, 211-First line, 212-Second line, 213-Boundary line, 221-First cross-section, 222-Second cross-section; e1, e2, e3, e4-Circular arc / elliptical arc;

[0029] 100 - Fluidized bed reactor; 101 - Tower tray / disc. Detailed Implementation

[0030] The specific embodiments of the present invention will be described in detail below. However, it should be noted that the scope of protection of the present invention is not limited to these specific embodiments, but is determined by the claims in the appendix.

[0031] All publications, patent applications, patents, and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings commonly understood by those skilled in the art. In case of conflict, the definitions in this specification shall prevail.

[0032] When this specification uses the prefixes “known to those skilled in the art,” “prior art,” or similar terms to derive materials, substances, methods, steps, apparatus, or components, the objects derived from such prefixes cover those commonly used in the art at the time of this application, but also include those that are not currently commonly used but will become generally recognized in the art as suitable for similar purposes.

[0033] In the context of this invention, all numerical values ​​of parameters (e.g., quantity or condition) should be understood to be modified by the term “about” in all cases, regardless of whether “about” actually appears before the numerical value.

[0034] In the context of this invention, "substantially" means that deviations that are acceptable or reasonable to those skilled in the art are permitted, such as deviations within ±2%, ±1%, ±0.5%, or ±0.1%.

[0035] In the context of this invention, projected area refers to the maximum area of ​​a component when projected onto each plane.

[0036] In the context of this invention, the flow direction refers to the flow direction of the fluid to be guided when the flow guiding member is in use, which is essentially a direction perpendicular to the horizontal plane.

[0037] In this paper, length refers to the length of a straight line segment between the center point of the distal section and the center point of the proximal section of a component (such as an elongated component), while the direction of length refers to the direction in which the straight line segment extends.

[0038] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0039] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “upper,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0040] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0041] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this instruction manual are based on weight, and the pressure is gauge pressure.

[0042] In the context of this invention, any two or more embodiments or aspects of this invention can be arbitrarily combined, and the resulting technical solutions are part of the original disclosure of this specification and also fall within the protection scope of this invention.

[0043] According to one embodiment of the present invention, a flow guiding member is provided. According to the present invention, the flow guiding member is particularly suitable as an internal component in a fluidized bed reactor, capable of generating strong vortices at the member, more effectively promoting gas-solid contact and mixing, and improving the quality of gas-solid fluidization. In the present invention, the flow guiding member is sometimes also referred to as a combined finned member.

[0044] According to one embodiment of the invention, the flow guiding member includes an elongated member. Here, an elongated member refers to a member with a significant length, generally whose length dimension is greater than its width or height dimension. In this invention, the elongated member is sometimes also referred to as a spanwise fin. The inventors of the invention have found that the arrangement of the elongated member helps to generate radial (and axial) vortices, with significantly enhanced radial transmission, for breaking up bubbles and particle clusters.

[0045] According to one embodiment of the invention, the elongated member has a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end. According to the invention, the proximal end refers to the mounting end of the elongated member on the flow guide member, while the distal end refers to the end opposite to the proximal end along the length direction of the elongated member, typically the free end of the elongated member.

[0046] According to one embodiment of the present invention, the elongated body includes at least a section such that when the elongated body is cut at any position along the flow direction within the section, only a pair of points furthest apart can be found on the outer periphery of the obtained cross-section (referred to as the total cross-section), referred to as the first point and the second point, respectively. According to the present invention, within the section, the total cross-section is not a symmetrical shape along the dividing line, such as a circle, triangle, rectangle, or teardrop shape. The inventors of the present invention have discovered that when the shapes on both sides of the dividing line of the cross-section of the elongated component are asymmetrical, when the airflow passes through the component, a velocity difference and pressure gradient are formed in the outer spatial region of the two asymmetrical shapes. The high-pressure airflow will roll and flow from the side with higher pressure through the far end of the elongated component to the side with lower pressure, forming vortices in the radial (spanwise) direction, enhancing the gas-solid transmission in the radial direction and effectively breaking up large bubbles in the bed.

[0047] According to one embodiment of the present invention, the outer periphery of the total cross-section is divided into a first line and a second line by the first point and the second point, with the straight line segment connecting the first point and the second point referred to as the dividing line. Let the length of the first line be L1 and the length of the second line be L2, then the value of L1 / L2 is greater than 1 (preferably 1.01-1.5 or 1.03-1.1). The inventors of the present invention have found that within the range of L1 / L2 values, it is more conducive to the formation of strong vortices in the radial direction, promoting the contact and mixing of the gas and solid phases.

[0048] According to one embodiment of the present invention, the flow guiding member satisfies condition 1): the first line is a curve (preferably a smooth curve, more preferably a smooth curve composed of multiple circular arcs / elliptical arcs), and the second line is a curve (preferably a smooth curve, more preferably a smooth curve composed of multiple circular arcs / elliptical arcs) or a straight line. The multiple segments are, for example, 2-6 segments, preferably 2-3 segments. According to condition 1, the curve can be a convex curve or a concave curve, but from the perspective of superior technical effect of the present invention, the curve is a convex curve. According to the present invention, there is no particular limitation on the specific shape of the curve; it can be a convex curve of any shape, but from the perspective of ease of manufacturing, it can be, for example, a part of a circle or ellipse (especially a minor arc). According to the present invention, the curve is more preferably a circular arc or elliptical arc of less than one-quarter length, or a streamlined curve of any shape, such as a smooth curve formed by connecting elliptical arcs (including circular arcs) with elliptical arcs (including circular arcs), preferably a streamlined curve composed of two quarter-elliptical arcs (including circular arcs), which is more conducive to the effective functioning of the flow guiding member of the present invention. The inventors of this invention discovered that a smooth curve allows airflow to pass more smoothly over the surface of the guide member, effectively reducing additional drag loss. The inventors also discovered that if the first line has an excessively large convex arc or a concave curve, trailing boundary layer separation may occur, resulting in additional pressure drag loss. When the second line is a concave curve, it can further enhance the pressure difference across the strip member, but whether this is beneficial for enhancing radial vortices is currently difficult to determine; when the second line is a convex curve, the elongated member has a greater thickness, resulting in better mechanical strength, wear resistance, durability, and a longer service life.

[0049] According to one embodiment of the present invention, the flow guiding member satisfies condition 2): the entire length of the dividing line lies within the total cross-section or on the outer periphery of the total cross-section. According to condition 2, either the first line or the second line is a straight line (but not simultaneously a straight line) or a convex curve, thereby ensuring that the dividing line does not fall outside the total cross-section, which is more conducive to the realization of the technical effect of the present invention. The inventors of the present invention have discovered that when the dividing line falls outside the total cross-section, for example, when the cross-section is crescent-shaped, the mechanical strength of the elongated member is poor, and the overall stability of the flow guiding member decreases.

[0050] According to one embodiment of the present invention, the flow guiding member satisfies condition 3): the portion of the total cross-section surrounded by the dividing line and the first line is called the first cross-section, and the portion of the total cross-section surrounded by the dividing line and the second line is called the second cross-section. Let the area of ​​the first cross-section be A1, and the area of ​​the second cross-section be A2. Then, the value of A1 / A2 (provided that neither the first line nor the second line is a straight line) is greater than 1 (preferably 1.1-21 or 2-9). The inventors of this invention have found that, according to condition 3, the cross-sectional area is directly related to the aforementioned curve shape, and structures that meet the specified range can be considered to have better effects in generating pressure differentials, suppressing boundary layer separation, and thus inducing radial vortices.

[0051] According to a preferred embodiment of the present invention, the first line and the second line are each composed of two elliptical arcs / circular arcs. The length ratio of the boundary lines corresponding to the two elliptical arcs / circular arcs constituting the first line is a1 / a2 = 0.05-0.6 (preferably 0.1-0.4), and the length ratio of the boundary lines corresponding to the two elliptical arcs / circular arcs constituting the second line is a1 / a2 = 0.05-0.6 (preferably 0.1-0.4). The inventors of the present invention have found that changes in the ratios of a1 / a2 and a3 / a4 do not affect the values ​​of A1 / A2 and L1 / L2. Within the aforementioned ranges of a1 / a2 and a3 / a4, it is beneficial to form radial vortices, break up bubbles, and enhance gas-solid mixing.

[0052] According to one embodiment of the present invention, the first line and the second line intersect at the first point and the second point respectively, forming a closed pattern. The inventors of the present invention have discovered that forming a closed pattern helps the airflow to pass over the first surface and the second surface corresponding to the first line and the second line respectively, utilizing the difference in surface area between the two to form a velocity difference and a pressure gradient, thereby generating radial vortices and enhancing turbulence.

[0053] According to one embodiment of the invention, the length of the elongated body is 50-400 mm (preferably 100-300 mm). According to the invention, the length of the segment is 30-100% of the length of the elongated body, preferably 70-100%, and more preferably the elongated body is substantially composed of the segment.

[0054] According to one embodiment of the present invention, when cutting the distal end of the elongated body along the flow direction, the obtained cross section is called the distal cross section, and when cutting the proximal end of the elongated body along the flow direction, the obtained cross section is called the proximal cross section. Let the length of the boundary line of the distal cross section be H1, and let the length of the boundary line of the proximal cross section be H2, then H1 / H2 = 0.005-1 (preferably 0.05-0.5). Furthermore, when cutting the elongated body at any two positions between the distal end and the proximal end along the flow direction, the two obtained cross sections are respectively called the first sampling cross section and the second sampling cross section, wherein the first sampling cross section is closer to the proximal end than the second sampling cross section. Let the length of the boundary line of the first sampling cross section be Hm, and let the length of the boundary line of the second sampling cross section be Hn, then Hm ≥ Hn (preferably Hm > Hn). According to a preferred embodiment of the present invention, the length of the dividing line of the cross-section of the elongated body gradually decreases continuously or intermittently from the proximal end to the distal end (preferably continuously and monotonically decreasing). The inventors of the present invention have discovered that when the elongated body is long, the dividing line of the cross-section at the distal end is long (which can be understood as being too wide), which will affect the structural stability of the elongated component.

[0055] According to this embodiment of the invention, H1 = 2-100 mm (preferably 15-50 mm), H2 = 50-400 mm (preferably 80-300 mm). Alternatively, at the proximal end, the total cross-sectional area (i.e., the total cross-sectional area of ​​the proximal cross section) is 400-25000 mm². 2 At the distal end, the total cross-sectional area (i.e., the total cross-sectional area of ​​the distal cross section) is 1-1500 mm. 2 Alternatively, at the proximal end, L1 = 60-600 mm (preferably 100-400 mm), and at the distal end, L1 = 3-150 mm (preferably 20-60 mm).

[0056] According to one embodiment of the present invention, the angle between the length direction of the elongated body and the dividing line is 30-90 degrees (preferably 60-90 degrees). Therefore, when the elongated component of the present invention is imagined as a long plate-like component, the plate-like component can be a straight plate or an inclined plate, with an inclined plate being preferred. The inventors of the present invention have discovered that within a certain angle range, the mutual coupling of radial and axial vortices is more conducive to producing a synergistic effect and better promoting uniform gas-solid distribution.

[0057] According to one embodiment of the present invention, the flow guiding member further includes a columnar member. In this invention, the columnar member is sometimes also referred to as a center rod. In this invention, the columnar member is provided for the purpose of fixing and mounting the elongated member.

[0058] According to one embodiment of the present invention, the elongated member and the columnar member are connected to each other at their proximal ends, such that the elongated member is arranged symmetrically or asymmetrically about the central axis of the columnar member on one or both sides of the columnar member. Preferably, when two or more elongated members are provided, the elongated members are arranged symmetrically about the central axis of the columnar member on both sides of the columnar member. The inventors of the present invention have found that the eddy current coverage area generated by multiple elongated members is larger. More preferably, the included angle between the length directions of two adjacent elongated members is greater than 0 degrees and not greater than 180 degrees (preferably 60-180 degrees, more preferably 90-150 degrees). The inventors of the present invention have found that this included angle range can both expand the eddy current range and avoid mutual interference.

[0059] According to one embodiment of the present invention, when the direction of the central axis of the columnar member is taken as the vertical direction, the angle between the dividing line and the vertical direction is 0 to 30° (preferably 0 to 10°) or 0 to -30° (preferably 0 to -10°). According to the present invention, when the elongated member is imagined as a long plate-like member, the plate-like member can be installed on the columnar member in a direction perpendicular to the horizontal plane (the included angle is 0 degrees), or it can be installed at an angle such that the included angle between its width or height direction and the central axis of the columnar member is greater than or less than 0 degrees. The inventors of the present invention have found that the effect of generating radial vortices is optimal within the range of the included angle. According to the present invention, when the flow guiding member is used, the flow guiding direction described in this specification corresponds to the direction of the central axis of the columnar member.

[0060] According to one embodiment of the present invention, the flow guiding member further includes a plate-like member. In the present invention, the plate-like member is sometimes also referred to as an axial fin. The inventors of the present invention have discovered that the windward end of the plate-like member has a cutting and breaking effect on moving bubbles, and can form a certain range of axial vortices at the trailing edge of the plate-like member, thereby enhancing gas-solid mixing.

[0061] According to one embodiment of the present invention, the sheet-like member and the columnar member are connected to each other, such that the sheet-like member is arranged symmetrically or asymmetrically about one side or both sides of the columnar member with respect to the central axis of the columnar member. Preferably, when two sheet-like members are arranged, the two sheet-like members are arranged symmetrically about the central axis of the columnar member on both sides of the columnar member; more preferably, the included angle between the two sheet-like members is 180 degrees. The inventors of the present invention have found that the axial vortices generated by arranging two symmetrical sheet-like members are basically symmetrically distributed and have a larger coverage area, resulting in stronger disturbances and being more conducive to bubble breakage.

[0062] According to one embodiment of the present invention, two or more (preferably two) of the sheet-like members and two or more (preferably two) of the elongated members are alternately arranged on the columnar member. Preferably, two adjacent elongated members are arranged symmetrically or asymmetrically about the plane direction of one sheet-like member on one or both sides of the sheet-like member. More preferably, two adjacent elongated members are arranged symmetrically about the plane direction of one sheet-like member on both sides of the sheet-like member. The inventors of the present invention have found that this arrangement is beneficial for enhancing the coupling of radial and axial vortices, better covering the gas-solid flow cross section of the fluidized bed, and promoting gas-solid contact mixing.

[0063] According to one embodiment of the present invention, when the direction of the central axis of the columnar member is taken as the vertical direction, the angle between the plane direction of the sheet-like member and the vertical direction is 0-30 degrees (preferably 0-10 degrees). The inventors of the present invention have found that the axial vortex generation effect is better within the range of this angle.

[0064] According to one embodiment of the present invention, there is no particular limitation on the projected shape of the sheet-like member, but it is generally selected from at least one of rectangular, triangular, trapezoidal, semi-elliptical, and irregular shapes, with a semi-elliptical shape being preferred. The inventors of the present invention have discovered that the semi-elliptical sheet-like member design, with its windward end being an arc resembling a blade shape, provides better breaking and cutting effects on bubbles while generating axial vortices.

[0065] According to one embodiment of the present invention, there is no particular limitation on the size of the sheet-like member, but it is generally 5-100mm wide, 10-300mm high, and 2-10mm thick.

[0066] According to one embodiment of the present invention, the ratio of the projected area of ​​the sheet-like member (axial fin) to the projected area of ​​the elongated member (spanwise fin) is 0.05-0.6. Here, the projected area of ​​the sheet-like member is the area of ​​its projected shape, while the projected area of ​​the elongated member is the area of ​​its projected shape on the horizontal plane when its boundary line is parallel to the horizontal plane. The inventors of the present invention have found that within this range of values, it is beneficial for the elongated member and the sheet-like member to form mutual coupling between vortices, thereby achieving a higher bubble breaking and mixing effect.

[0067] According to one embodiment of the present invention, the flow guiding member further includes a connecting rod. According to the present invention, one or more of the columnar members are fixedly disposed on the connecting rod. The function of the connecting rod is to install the flow guiding member of the present invention onto the shell of a container, such as a fluidized bed reactor.

[0068] According to one embodiment of the present invention, the spacing between the plurality of columnar members on the connecting rod (based on the central axis) is 100-1000 mm (preferably 200-400 mm). The inventors of the present invention have discovered that an appropriate spacing can suppress mutual interference between the eddies generated by each member and maximize the eddy current intensity, thereby enhancing gas-solid mixing.

[0069] According to one embodiment of the present invention, the angle between the central axis of the connecting rod and the central axis of the columnar member is 45-90 degrees, preferably about 90 degrees, that is, it is installed substantially vertically.

[0070] According to one embodiment of the present invention, multiple connecting rods can be arranged in the same horizontal plane. Preferably, the horizontal projections of the elongated members on opposite sides of two adjacent connecting rods are substantially parallel. The inventors of the present invention have found that the preferred arrangement of the elongated members can be approximately understood as the members on two adjacent connecting rods being staggered along their length directions, thereby enhancing the staggered distribution of gas-solid flow in the horizontal direction and improving radial transmission and debubbling efficiency.

[0071] According to one embodiment of the present invention, a fluidized bed reactor is also disclosed, comprising a shell and flow guiding members disposed within the shell. Here, the flow guiding members include those described in any of the foregoing or subsequent descriptions of the present invention. Preferably, all flow guiding members installed in the fluidized bed reactor are those described in any of the foregoing or subsequent descriptions of the present invention. During installation, the flow guiding members are arranged in multiple layers (e.g., 2-20 layers) along the central axis of the reactor. Preferably, the vertical spacing between each layer (based on the central axis of the connecting rod) is 0.1-0.25 times the diameter of the reactor. The inventors of the present invention have found that this vertical spacing allows rising bubbles to break up in a timely manner, effectively preventing the bubbles from re-aggregating due to excessive vertical spacing of the flow guiding members, while avoiding increased fluidized bed construction costs due to excessively small spacing or too many distributors.

[0072] According to one embodiment of the present invention, the central axes of the connecting rods of adjacent two layers of flow guiding members form an included angle. Preferably, the included angle is 90 degrees. The inventors of the present invention have discovered that the vertical arrangement of the connecting rods of adjacent two layers allows the gas and solid phases to flow in a crisscrossing and meandering manner in the axial direction. Under the action of the flow guiding members, bubbles and particle clusters are broken up, enhancing the gas-solid contact effect.

[0073] According to one embodiment of the present invention, the reactor further includes other internal components such as a gas distributor, without particular limitation. According to the present invention, as an example of arrangement, the lowest layer of the flow guiding member is disposed above the gas distributor. Furthermore, the vertical distance between the lowest layer of the flow guiding member and the gas distributor (based on the central axis of the connecting rod) is 0.1-0.2 times the diameter of the reactor. The inventors of the present invention have discovered that the installation height of the lowest layer of the flow guiding member effectively suppresses the growth and coalescence of bubbles during their axial ascent after leaving the distributor.

[0074] According to one embodiment of the present invention, multiple rows (e.g., 9-39 rows) of the flow guiding members can be arranged within the same cross-section of the reactor. Preferably, the horizontal spacing between each row (based on the central axis of the connecting rod) is 0.025-0.1 times the diameter of the reactor. The inventors of the present invention have discovered that the above-mentioned horizontal spacing can utilize a limited number of flow guiding members to cover a sufficiently large flow cross-section to meet the bubble breaking requirements.

[0075] In the context of this invention, the pressure standard deviation Sd characterizes the intensity of pressure pulsation within the reactor. The inventors of this invention have found that a larger Sd indicates poorer gas-solid contact within the fluidized bed. This invention aims to achieve the minimum pressure standard deviation Sd value, which results in the highest gas-solid fluidization quality. According to this invention, Sd ≤ 8 kPa (preferably ≤ 4 kPa).

[0076] Where Sd is the standard deviation of pressure at any measurement point; N is the number of sampled data; and Pi is the transient pressure at any time. This represents the average pressure. P' represents the pressure fluctuation value.

[0077] According to one embodiment of the present invention, a fluidized bed reaction method is also provided, comprising a step of carrying out a chemical reaction in a fluidized bed reactor as described above or below. Here, the chemical reaction may be a cold hydrogenation reaction of silicon tetrachloride, an organosilicon synthesis reaction, or a hydrogenation reaction of nitrobenzene to aniline, etc.

[0078] According to one embodiment of the present invention, the reaction conditions for the cold hydrogenation reaction include: a reaction temperature of 450-620°C, a reaction pressure of 2.0-4.0 MPaG, and a gas apparent linear velocity of 0.05-0.8 m / s.

[0079] The invention will be further described below based on the accompanying drawings, but the invention is not limited to these drawings.

[0080] As shown in Figures 1 to 5, the present invention provides a flow guiding member for use in a fluidized bed reactor to improve gas-solid contact and mixing efficiency. This flow guiding member 1, used to generate strong eddies within the reactor and improve gas-solid fluidization quality, includes at least an elongated member 11, which refers to a member with a significant length. This elongated member is disposed above the fluidized bed of solid particles (not shown in the figures) and extends radially along the axial airflow (i.e., the mainstream airflow direction, referring to Figure 7, i.e., the airflow from bottom to top along the reactor's axial direction). This elongated member is sometimes also called a spanwise fin. The elongated member has a proximal end 113 and a distal end 114, and an elongated body 115 extending between the proximal and distal ends. The proximal end 113 refers to the mounting end of the elongated member 11 on the flow guiding member 1, while the distal end 114 refers to the end opposite the proximal end, typically the free end of the elongated member.

[0081] Furthermore, as shown in Figure 6, the elongated body includes at least the following section: when the elongated member is cut at any position along the plane parallel to the end plane of the spanwise fin (or the plane perpendicular to the horizontal plane and parallel to the connecting rod) within the section, only a pair of points furthest apart can be found on the outer periphery of the obtained cross section (called the total cross section), which are respectively called the first point 201 and the second point 202.

[0082] Furthermore, the outer periphery of the total cross-section is divided into a first line 211 and a second line 222 by the first and second points, respectively. The straight line segment connecting the first and second points is called the dividing line 213. The length L1 of the first line is greater than the length L2 of the second line, that is, the L1 / L2 value is greater than 1, preferably 1.01-1.5, and more preferably 1.03-1.1. With this structural design, the airflow velocity flowing through the first surface 111 (see Figure 1) corresponding to the first line will be greater than the airflow velocity flowing through the second surface 112 (see Figure 1) corresponding to the second line. The velocity difference can form a pressure gradient between the first and second surfaces (that is, the first surface 111 has a certain negative pressure effect). On this basis, the high-pressure airflow of the second surface 112 can roll and flow along the spanwise fins 11 to the lower pressure first surface 111. Combined with the mainstream direction of the fluid (refer to the airflow direction shown in Figure 1), a strong vortex is formed, as shown in the streamline distribution in Figure 10. This strong vortex can enhance the radial transfer of gas and solid, improve the gas-solid fluidization quality and gas-solid transfer efficiency in the fluidized bed, and thus improve the reaction efficiency. In addition, while forming a strong radially transferred vortex, the elongated member 11 can break and cut bubbles because the airflow is divided at the windward end of the elongated member 11. Under the action of the strong vortex, it can effectively prevent small bubbles from merging into large bubbles.

[0083] Furthermore, on the cross-section 2 of the elongated body, the first line 211 is a curve, preferably a smooth curve, more preferably a smooth curve formed by connecting multiple circular / elliptical arcs; the second line 212 is a curve or a straight line, preferably a smooth curve, more preferably a smooth curve formed by connecting multiple circular / elliptical arcs; as shown in Figure 6. The curve is more conducive to the smooth flow of air over the surface of the component, reducing additional resistance loss.

[0084] Furthermore, the entire length of the dividing line 213 on the cross-section of the elongated body is located within the total cross-section or on the outer periphery of the total cross-section.

[0085] Furthermore, the portion enclosed by the dividing line 213 and the first line 211 on the cross-section of the elongated body is called the first cross-section 221, and the portion enclosed by the dividing line 213 and the second line 212 is called the second cross-section 222, as shown in Figure 6; the ratio of the area A1 of the first cross-section to the area A2 of the second cross-section (provided that neither the first line nor the second line is a straight line) A1 / A2>1, preferably 1.1-21 or 2-9.

[0086] Furthermore, if the shape constituting the first line and / or the second line is a circular arc or an elliptical arc or a combination thereof, when the first line and the second line are each composed of two circular arcs or elliptical arcs, the length ratio of the aforementioned dividing line corresponding to the two circular arcs / elliptical arcs constituting the first line is a1 / a2 = 0.05-0.6 (preferably 0.1-0.4), and the length ratio of the aforementioned dividing line corresponding to the two circular arcs / elliptical arcs constituting the second line is a3 / a4 = 0.05-0.6 (preferably 0.1-0.4).

[0087] As further shown in Figure 6, the first line 211 and the second line 212 on the cross-section of the elongated body intersect at the first point 201 and the second point 202 respectively, forming a closed shape. This is used to guide the airflow through the first surface 111 and the second surface 112 with different surface areas, forming a velocity difference and pressure gradient, generating radial vortices, and enhancing turbulence and radial mixing.

[0088] Further, the length of the elongated body 115 is 50-400 mm, preferably 100-300 mm. The present invention finds that the length of the aforementioned section is 30-100% of the length of the elongated body, preferably 70-100%, and the effect is better when the elongated body is substantially composed of the aforementioned section. The ratio H1 / H2 between the length H1 of the boundary line of the distal cross-section formed by perpendicularly cutting the distal end of the strip member and the length H2 of the boundary line of the proximal cross-section formed by perpendicularly cutting the proximal end of the strip member is 0.005-0.1, preferably 0.05-0.5. Further, when cutting the elongated body at any two positions between the distal end and the proximal end along the flow direction, the two obtained cross-sections are respectively called the first sampling cross-section and the second sampling cross-section, wherein the first sampling cross-section is closer to the proximal end than the second sampling cross-section. Let the length of the boundary line of the first sampling cross-section be Hm, and let the length of the boundary line of the second sampling cross-section be Hn, then Hm ≥ Hn (preferably Hm > Hn). Furthermore, the length of the dividing line of the cross-section of the elongated body gradually decreases continuously or intermittently from the proximal end to the distal end (preferably continuously decreasing monotonically).

[0089] Further, the length of the dividing line H1 of the distal cross-section formed by the vertical cut at the distal end of the strip member is 2-100 mm, preferably 15-50 mm; the length of the dividing line H2 of the proximal cross-section formed by the vertical cut at the proximal end of the strip member is 50-400 mm, preferably 80-300 mm. Further, the total cross-sectional area of ​​the proximal section is 400-25000 mm². 2 Preferred size: 600-13000mm 2 The total cross-sectional area of ​​the distal section is 1-1500 mm. 2 50-600mm is preferred. 2 Furthermore, the length of the first line on the proximal cross-section is L1 = 60-600 mm, preferably 100-400 mm, and the length of the first line on the distal cross-section is L1 = 3-150 mm, preferably 20-60 mm.

[0090] As shown in Figure 3, the elongated component can be a straight plate or an inclined plate; the angle between the length direction of the elongated body and the dividing line on the cross-section is 30-90 degrees, preferably 60-90 degrees, which is more conducive to the generation of radial vortices.

[0091] Furthermore, the flow guiding component includes a columnar component for fixing the elongated component. The proximal end of the elongated component is connected to the columnar component, and the components are arranged symmetrically or asymmetrically on one or both sides of the columnar component with the central axis as the axis. Symmetrical arrangement is preferred, so that the vortices formed by the elongated components on both sides are also basically symmetrical, avoiding unwanted local turbulence. When multiple elongated components are used, the included angle between adjacent components is greater than 0 degrees and not greater than 180 degrees, preferably 60-180 degrees, and more preferably 90-150 degrees. Using multiple elongated components is mainly to generate a sufficiently large vortex coverage area, but the number should not be too large to avoid mutual interference and increased component production costs.

[0092] Furthermore, the angle between the dividing line of the elongated body's cross-section and the central axis (vertical direction) of the columnar member is 0-30 degrees, preferably 0-10 degrees. That is, when the central axis of the columnar member is vertical, the elongated member can be installed on the columnar member in a direction perpendicular to the horizontal plane (width direction), as shown in Figure 4, or it can be installed at an angle so that its width direction forms a certain angle with the horizontal direction.

[0093] Further, as shown in Figures 1-5, the flow guiding component 1 also includes a plate-shaped component 12, which is also an axial fin. The plate-shaped component 12 is connected to the columnar component 10 and is arranged symmetrically or asymmetrically with respect to the central axis of the columnar component. Further still, two or more plate-shaped components and two or more elongated components are alternately arranged on the columnar component, preferably with adjacent elongated components arranged symmetrically or asymmetrically with respect to the plane direction of one plate-shaped component, as shown in Figure 5. Studies have found that when the central axis of the columnar component is vertical, an angle of 0-30 degrees between the plane direction of the plate-shaped component and the vertical direction is more effective, preferably 0-10 degrees. Further, the projection surface of the plate-shaped component can be composed of at least one of rectangular, triangular, trapezoidal, semi-elliptical, or irregular shapes, preferably semi-elliptical. The windward section of the elliptical plate-shaped fin has a blade-like arc shape, which provides a better cutting and breaking effect on bubbles. There are no particular restrictions on the size of sheet-like components; they are typically 5-100mm wide, 10-300mm high, and 2-10mm thick.

[0094] The study found that when the airflow flows upward through the guide member 1, the elongated members 11 arranged on both sides in Figure 4 can generate radial vortices, while the symmetrically arranged sheet-like members 12 in Figure 4 can generate axial vortices. The two vortices are further enhanced after they meet and mix, thus achieving radial and axial gas-solid transfer. The combined use of the elongated members 11 and the sheet-like members 12 has a synergistic effect; the strong vortices generated by their combined action result in better gas-solid contact and mixing. The ratio of the projected area of ​​the sheet-like members to that of the elongated members is 0.05-0.6.

[0095] As further shown in Figures 1, 2, and 5, the flow guiding component also includes a connecting rod 13. This serves two purposes: firstly, to fix the columnar component, and secondly, to install the flow guiding component onto the wall of the fluidized bed reactor 100 along the vertical direction of the airflow (radial direction of the reactor 100), i.e., to fix it onto the fluidized bed tray disc 101 (refer to Figure 7). The spacing between the multiple columnar components (based on the central axis) is 100-1000 mm, preferably 200-400 mm; the angle between the central axis of the connecting rod and the central axis of the columnar component is 45-90 degrees, preferably approximately 90 degrees, i.e., vertical installation is more effective. The columnar component 10 and the connecting rod 13 can be manufactured as a single piece. The elongated component 11 and the sheet-like component 12 can be integrally formed with the columnar component 10, or they can be installed on the columnar component 10 by insertion and fixing, depending on site requirements.

[0096] Further, as shown in Figures 7 to 9, the present invention also provides a fluidized bed reactor 100, which can utilize the flow guiding member described in any of the foregoing or subsequent descriptions of the present invention to obtain strong eddies within the reactor and improve the quality of gas-solid fluidization. Further, preferably but not limitingly, in order to obtain strong eddies throughout the effective space of the fluidized bed reactor 100, the flow guiding member of the present invention can be arranged in layers along the central axis of the reactor. Specifically, for example, 2-20 layers can be arranged, and the vertical distance between each layer (based on the central axis of the connecting rod) is 0.1-0.25 times the diameter of the reactor. The central axes of the connecting rods of adjacent layers of flow guiding members form an angle, preferably 90 degrees, that is, the connecting rods of adjacent layers are arranged perpendicularly, as shown in Figure 7. Furthermore, multiple rows of flow guiding components can be arranged within the same cross-section of the reactor, such as 9-39 rows, as shown in Figure 8; the horizontal spacing between each row (based on the central axis of the connecting rod) is 0.025-0.1 times the reactor diameter; the horizontal projections of the elongated components on opposite sides of two adjacent connecting rods are basically parallel, as shown in Figure 9.

[0097] Furthermore, the fluidized bed reactor 100 may also include a gas distributor and a cyclone separator (not shown in the figure). The gas distributor is located below the solid particle bed and forms a uniform upward airflow in a jet pattern. The lowest guiding member is located above the gas distributor, and its vertical distance from the gas distributor (based on the central axis of the connecting rod) is 0.1-0.2 times the diameter of the reactor. The cyclone separator is located above the area where the combined finned member is located. It receives gas carrying solid particles and performs gas-solid separation. The separated solid particles return to the dense phase zone of the bed via the cyclone feed leg (not shown in the figure), while the separated gas flows out of the reactor for use in the next process unit.

[0098] Furthermore, the present invention also provides a fluidized bed reaction method, comprising the steps of carrying out a chemical reaction using the fluidized bed reactor 100 described above or below. Here, the chemical reaction may be a cold hydrogenation reaction of silicon tetrachloride, an organosilicon synthesis reaction, or a hydrogenation reaction of nitrobenzene to aniline, etc. The fluidized bed reactor 100 is equipped with and uses the aforementioned combined finned components, comprising the following steps:

[0099] In step S101, the gas enters the reactor from bottom to top and comes into full contact with and mixes with the solid particles, so that the solid particles on the bed are in a fluidized state, that is, the gas pushes the particles to flow in the fluidized bed reactor 100 in the mainstream direction from bottom to top.

[0100] In step S102, when the gas and solid flow through the guide member 1, the unique structural design of the elongated member 11 can form radial vortices, which enhance the radial transmission of gas and solid. The airflow flowing through the sheet member forms axial vortices. The two have a synergistic effect, which can enhance the turbulence intensity, effectively break up large bubbles in the fluidized bed, and make the gas-solid contact and mixing effect better, thereby effectively improving the gas-solid fluidization quality and gas-solid transmission efficiency.

[0101] Furthermore, prior to step S101, a step may be included to uniformly distribute the gas source into the fluidized bed reactor using a gas distributor, thereby obtaining a uniform, upward-flowing gas flow at the bottom of the reactor.

[0102] Furthermore, after step S102, a gas-solid separation step may be included to separate the gas carrying some solid particles. The separated solid particles are returned to the dense phase region of the bed, and the separated gas flows out of the reactor for subsequent reactions.

[0103] The method described above in this invention can be applied to the cold hydrogenation reaction in the preparation of polycrystalline silicon. When preparing polycrystalline silicon using the method of this invention, the gas source for the cold hydrogenation reaction can be at least two of silicon tetrachloride, hydrogen, and hydrogen chloride; the solid particles can be silicon powder. The reaction temperature of the cold hydrogenation reaction can be 450-620℃, the pressure can be 2.0-4.0 MPa, and the apparent gas linear velocity can be 0.05-0.8 m / s.

[0104] Example

[0105] The present invention will be further described in detail below with reference to examples and comparative examples, but the present invention is not limited to these examples.

[0106] Example 1

[0107] A fluidized bed reactor 100 is used for cold hydrogenation reaction, and as shown in Figure 7, a flow guiding component 1 to enhance gas-solid contact is installed in the reactor 100. The flow guiding component consists of elongated components, sheet-like components, columnar components, and connecting rods. The elongated components and sheet-like components are connected to the columnar components, and the columnar components are fixedly mounted on the connecting rods.

[0108] The gas source enters the fluidized bed reactor 100 through a gas distributor, fully contacting and mixing with the solid particles in the reactor, propelling the particles to flow within the fluidized bed reactor. When the gas and solid flow passes through the guide member, the length difference between the first and second lines on the cross-section of the elongated member causes a pressure gradient to form between the airflows flowing over the two surfaces of the elongated member due to the velocity difference. The high-pressure airflow rolls along the far end of the elongated member to the lower-pressure side, as shown in the streamline distribution in Figure 10. Combined with the mainstream direction of the fluid, this forms a strong vortex. This vortex enhances the radial transfer of gas and solid, effectively breaking up large bubbles in the fluidized bed, thereby improving the gas-solid fluidization quality and gas-solid transfer efficiency. Similarly, the sheet-like member generates a strong vortex within its influence area, enhancing the gas-solid transfer efficiency in that area. The two vortices have a synergistic effect through coupling. Above the fluidized bed reactor 100, due to particle entrainment and separation, some particles are separated by the cyclone separator. The gas flows out of the fluidized bed reactor and enters the subsequent chemical unit, while the particles flow into the dense phase zone of the fluidized bed reactor 100 through the cyclone feed leg after separation.

[0109] The combined fin component used to enhance gas-solid contact consists of a unit structure as shown in Figures 1-6, which is repeatedly arranged to form a tray-shaped integral component as shown in Figure 7.

[0110] The elongated component has a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end. The first and second lines of any cross-section of the segment included in the elongated body are convex curves, each formed by two elliptical arcs connected together. Referring to Figure 6, the first line 211 is formed by two quarter-elliptical arcs e1 and e2, and the second line 212 is formed by quarter-elliptical arcs e3 and e4. The first and second lines intersect to form a closed figure. The length ratio of the dividing line corresponding to elliptical arcs e1 and e2 is a1 / a2 = 0.176, and the length ratio of the dividing line corresponding to elliptical arcs e3 and e4 is a3 / a4 = 0.136. Correspondingly, the length ratio of the first and second elliptical arcs is L1 / L2 = 1.08, and the area ratio of the first cross-section to the second cross-section is A1 / A2 = 4.5. The total cross-sectional area of ​​the proximal end (mounting end) is 863.5 mm². 2 L1 = 110.3 mm, and the total cross-sectional area at the distal end is 77.7 mm². 2L1 = 33.1 mm; the length of the cuboid body is 100 mm, and the length of the segment with the above characteristics is 100% of the length of the cuboid body; the length of the dividing line of the distal cross-section of the cuboid body is H1 = 30 mm, and the ratio of the length of the dividing line of the proximal cross-section to the length of the dividing line is H1 / H2 = 0.3; the angle between the length direction of the cuboid body and the dividing line is 68.0°; the angle between the length directions of two adjacent cuboid members is 120° (2 in total, see Figure 9); the angle between the dividing line and the vertical direction (the central axis of the columnar member) is 5°.

[0111] Two semi-elliptical sheet-like components (30mm wide, 100mm high, and 2mm thick, with a projected area ratio of 0.36 between the sheet-like component and the elongated component) are installed axially symmetrically on both sides of the columnar component (refer to Figure 9). The angle between the planar direction of the sheet-like component and the vertical direction (central axis of the columnar component) is 0°. The spacing between the columnar components on the same connecting rod is 200mm. The angle between the central axis of the connecting rod and the central axis of the columnar component is 90°. The longitudinal directions of the spanwise fins on opposite sides of two adjacent connecting rods are substantially parallel. The vertical spacing between each layer (10 layers in this embodiment) of the flow guiding components is 0.15 times the reactor diameter, and the central axes of the connecting rods of two adjacent layers of flow guiding components form an angle of 90°. The bottommost layer of flow guiding components is located above the gas distributor, and the vertical spacing between it and the gas distributor is 0.15 times the reactor diameter. The horizontal spacing between two adjacent rows of flow guiding components within the same cross-section of the reactor is 0.05 times the reactor diameter.

[0112] The reaction gases in the dense phase zone of the fluidized bed reactor consist of silicon tetrachloride, hydrogen, and hydrogen chloride; the reaction particles are silicon powder; the reaction temperature is 550℃; the operating pressure is 3 MPaG; and the apparent linear velocity of the gas is 0.2 m / s. The calculated pressure standard deviation Sd is 2.63 kPa.

[0113] Example 2

[0114] Similar to Example 1, the only difference is that the elliptical arcs e1 and e2 share the same axis b1, so that the length ratio of the first line to the second line is L1 / L2 = 1.22 (A1 / A2 = 11), and the pressure standard deviation Sd is 4.13 kPa.

[0115] Example 3

[0116] Similar to Example 1, the only difference is that the common axis b1 of the elliptical arcs e1 and e2 is shortened, so that the length ratio of the first line to the second line is L1 / L2 = 1.02 (A1 / A2 = 2), and the pressure standard deviation Sd is 2.91 kPa.

[0117] Example 4

[0118] Similar to Example 1, the only difference is that the elliptical arcs e1 and e2 share the same axis b1, so that the length ratio of the first line to the second line is L1 / L2 = 1.16 (A1 / A2 = 8), and the pressure standard deviation Sd is 3.35 kPa.

[0119] Example 5

[0120] Similar to Example 1, the only difference is that the first line is a broken line and the second line is a straight line (i.e., the dividing line). The first line and the second line form a right triangle with the second line as the right angle side and containing a 12-degree angle. The pressure standard deviation Sd is 6.56 kPa.

[0121] Example 6

[0122] Similar to Example 1, the only difference is that the first line is a broken line and the second line is a smooth convex arc. The first line and the dividing line form a right triangle with the dividing line as the right angle side and containing a 9-degree angle. The second line is a 1 / 12 arc with the dividing line as the chord. The pressure standard deviation Sd is 7.33 kPa.

[0123] Example 7

[0124] Similar to Example 1, the only difference is that the cross-section is crescent-shaped. Taking the dividing line in Example 1 as the chord, the first line is a one-sixth convex arc, and the second line is a quarter arc. The ratio of the arc diameter D1 constituting the first line to the arc diameter D2 constituting the second line is D1 / D2 = 0.71, and the pressure standard deviation Sd is 7.43 kPa.

[0125] Example 8

[0126] Similar to Example 1, the only difference is that the common axis b1 of the elliptical arcs e1 and e2 is shortened, so that the area ratio of the first section to the second section is A1 / A2 = 1.05 (L1 / L2≈1.001), and the pressure standard deviation Sd is 3.51 kPa.

[0127] Example 9

[0128] Similar to Example 1, the only difference is that the common axis b1 of elliptical arcs e1 and e2 is increased, and the common axis b2 of elliptical arcs e3 and e4 is shortened, so that the area ratio of the first section to the second section is A1 / A2 = 22 (L1 / L2 = 1.24), and the pressure standard deviation Sd is 4.23 kPa.

[0129] Example 10

[0130] Similar to Example 1, the only difference is that the elliptical arcs e1 and e2 share the same axis b1, so that the area ratio of the first section to the second section is A1 / A2 = 10 (L1 / L2 = 1.2), and the pressure standard deviation Sd is 3.09 kPa.

[0131] Example 11

[0132] Similar to Example 1, the only difference is that the ratio of the lengths of the dividing lines corresponding to the elliptical arcs e1 and e2 is a1 / a2 = 0.081, and the pressure standard deviation Sd is 2.73 kPa.

[0133] Example 12

[0134] Similar to Example 1, the only difference is that the ratio of the lengths of the dividing lines corresponding to the elliptical arcs e1 and e2 is a1 / a2 = 0.67, and the pressure standard deviation Sd is 3.33 kPa.

[0135] Example 13

[0136] Similar to Example 1, the only difference is that the ratio of the lengths of the dividing lines corresponding to the elliptical arcs e3 and e4 is a3 / a4 = 1, and the pressure standard deviation Sd is 2.68 kPa.

[0137] Example 14

[0138] Similar to Example 1, the only difference is that the common axis b1 of the elliptical arcs e1 and e2 is shortened, making the total area of ​​the near-end cross-section 545 mm². 2 The total cross-sectional area at the distal end is 49.5 mm². 2 The pressure standard deviation Sd is 2.85 kPa.

[0139] Example 15

[0140] Same as Example 1, except that the proximal L1 = 60.3 mm, the distal L = 18.1 mm, and the pressure standard deviation Sd is 3.36 kPa.

[0141] Example 16

[0142] Same as Example 1, except that the elongated body is 50 mm long and the pressure standard deviation Sd is 4.35 kPa.

[0143] Example 17

[0144] Similar to Example 1, the only difference is that the ratio of the length of the dividing line of the distal cross section to the length of the proximal cross section of the elongated body is H1 / H2 = 1.2 (keeping the proximal H2 unchanged), and the pressure standard deviation Sd is 4.79 kPa.

[0145] Example 18

[0146] Similar to Example 1, the only difference is that the ratio of the length of the dividing line of the far end cross section to the length of the near end cross section of the elongated body is H1 / H2 = 0.03, and the pressure standard deviation Sd is 4.37 kPa.

[0147] Example 19

[0148] Similar to Example 1, the only difference is that the ratio of the length of the dividing line of the far end cross section to the length of the near end cross section of the elongated body is H1 / H2 = 0.7, and the pressure standard deviation Sd is 3.72 kPa.

[0149] Example 20

[0150] Similar to Example 1, the only difference is that the ratio of the length of the dividing line of the far end cross section to the length of the near end cross section of the elongated body is H1 / H2 = 1, and the pressure standard deviation Sd is 4.23 kPa.

[0151] Example 21

[0152] Same as Example 1, except that the length of the dividing line is shortened, H1 = 18 mm, H2 = 60 mm, and the pressure standard deviation Sd is 3.11 kPa.

[0153] Example 22

[0154] Similar to Example 1, the only difference is that the angle between the length direction of the elongated body and the dividing line is 20°, and other angles vary accordingly with geometric constraints. The pressure standard deviation Sd is 3.62 kPa.

[0155] Example 23

[0156] Similar to Example 1, the only difference is that the angle between the length direction of the elongated body and the dividing line is 50°, and other angles vary accordingly with geometric constraints. The pressure standard deviation Sd is 3.06 kPa.

[0157] Example 24

[0158] Similar to Example 1, the only difference is that the included angle between the length directions of two adjacent elongated components is 45° and the pressure standard deviation Sd is 6.25 kPa.

[0159] Example 25

[0160] Similar to Example 1, the only difference is that the included angle between the length directions of two adjacent elongated components is 75° and the pressure standard deviation Sd is 5.53 kPa.

[0161] Example 26

[0162] Similar to Example 1, the only difference is that the included angle between the length directions of two adjacent elongated components is 180°, and the included angle between the elongated component and the dividing line is 90°, with a pressure standard deviation Sd of 2.73 kPa.

[0163] Example 27

[0164] Similar to Example 26, the only difference is that the elliptical arcs e1 and e2 share the same axis b1, and the elliptical arcs e3 and e4 share the same axis b2, so that the length ratio of the first line to the second line is L1 / L2 = 1.46 (A1 / A2 = 70), and the pressure standard deviation Sd is 4.51 kPa.

[0165] Example 28

[0166] Similar to Example 1, the only difference is that the angle between the dividing line of the elongated body cross section and the vertical direction (the central axis of the columnar member) is 12°, and the pressure standard deviation Sd is 4.63 kPa.

[0167] Example 29

[0168] Similar to Example 1, except that no sheet-like components are provided on the columnar component, and the pressure standard deviation Sd is 6.01 kPa.

[0169] Example 30

[0170] Similar to Example 1, except that only one plate-shaped member is provided on the columnar member, and the pressure standard deviation Sd is 5.34 kPa.

[0171] Example 31

[0172] Similar to Example 1, the only difference is that only one elongated member is provided on the columnar member, and the pressure standard deviation Sd is 7.61 kPa.

[0173] Example 32

[0174] Similar to Example 1, the only difference is that the angle between the planar direction of the sheet member and the vertical direction (the central axis of the column member) is 12°, and the pressure standard deviation Sd is 4.27 kPa.

[0175] Example 33

[0176] Similar to Example 1, the only difference is that the structural dimensions of the sheet-like component are changed (width is 6mm, height is 60mm, thickness is 2mm), the ratio of its projected area to the projected area of ​​the elongated component is 0.043, and the pressure standard deviation Sd is 4.26KPa.

[0177] Example 34

[0178] Similar to Example 1, the only difference is that the spacing between the columnar components on the same connecting rod is 80 mm, and the pressure standard deviation Sd is 2.91 kPa.

[0179] Example 35

[0180] Similar to Example 1, the only difference is that the spacing between the columnar components on the same connecting rod is 150 mm, and the pressure standard deviation Sd is 2.68 kPa.

[0181] Example 36

[0182] Similar to Example 1, the only difference is that the spacing between the columnar components on the same connecting rod is 600 mm, and the pressure standard deviation Sd is 4.92 kPa.

[0183] Example 37

[0184] Similar to Example 1, the only difference is that the angle between the central axis of the connecting rod and the central axis of the columnar member is 60°, and the pressure standard deviation Sd is 5.12 kPa.

[0185] Example 38

[0186] Similar to Example 1, the only difference is that the vertical spacing between two adjacent flow guide components is 0.35 times the reactor diameter, and the pressure standard deviation Sd is 4.13 kPa.

[0187] Example 39

[0188] Similar to Example 1, the only difference is that the vertical distance between the bottommost flow guide component and the gas distributor is 0.3 times the reactor diameter, and the pressure standard deviation Sd is 3.51 kPa.

[0189] Example 40

[0190] Similar to Example 1, the only difference is that the spacing between two adjacent rows of flow guide members in the same cross section is 0.25 times the reactor diameter, and the pressure standard deviation Sd is 6.03 kPa.

[0191] Comparative Example 1

[0192] Similar to Example 1, the only difference is that the cross-section of the elongated body is circular. In any cross-section along the length of the elongated body, the diameter (boundary line) of the circle is 20 mm and the standard deviation of pressure Sd is 8.73 kPa.

[0193] Comparative Example 2

[0194] Similar to Example 1, the only difference is that the cross-section of the elongated body is rectangular. In any cross-section along the length of the elongated body, the side length of the rectangle along the vertical direction (the direction of the central axis of the columnar member) is 50 mm, the side length perpendicular to the central axis is 20 mm, and the pressure standard deviation Sd is 8.92 kPa.

[0195] Comparative Example 3

[0196] Similar to Example 1, the only difference is that the cross-section of the elongated body is triangular. In any cross-section along the length of the elongated body, the triangle is an inverted isosceles triangle. The length of the base perpendicular to the central axis of the columnar member is 20mm, the height of the triangle along the central axis of the columnar member is 50mm, and the pressure standard deviation Sd is 8.21KPa.

[0197] Comparative Example 4

[0198] Similar to Example 1, the only difference is that the cross-section of the elongated body is teardrop-shaped. At any cross-section along the length of the elongated body, the upper part of the teardrop shape is an isosceles triangle with a base length of 20mm and a height of 50mm, and the lower part is a semicircle with a diameter of 20mm. The base of the triangle coincides with the diameter of the semicircle and is perpendicular to the central axis of the columnar component. The pressure standard deviation Sd is 8.33KPa.

[0199] Comparative Example 5

[0200] Similar to Example 1, the only difference is that the first line and the second line do not intersect at the first point and the second point. Referring to Figure 6, the elongated component is divided into two parts along the central axis 213, with a distance of 5 mm between them and a pressure standard deviation Sd of 8.11 kPa.

[0201] Comparative Example 6

[0202] Similar to Example 1, the only difference is that the first line and the second line do not intersect at the first point, but intersect at the second point. Referring to Figure 6, they intersect at point 201 and do not intersect at point 202. The angle formed by the first cross-section and the second cross-section is 5 degrees, and the pressure standard deviation Sd is 8.13 kPa.

[0203] Comparative Example 7

[0204] Similar to Example 1, the only difference is that the first line is a concave curve and the second line is also a concave curve (the cross-section is similar to a dumbbell shape). The first and second lines are symmetrically distributed arcs, with the widest length at both ends being 20 mm and the narrowest length at the center being 5 mm. The pressure standard deviation Sd is 8.26 kPa.

[0205] As can be seen from the above comparison, when the structural indicators of each component are selected from the data in Example 1, the pressure standard deviation Sd value is the smallest, so it is the relatively optimal solution. When only other flow guiding components within the preferred range are used, good gas-solid fluidization quality can also be guaranteed. Although the technical effect is not as good as Example 1, it is far better than the comparative example.

Claims

1. A flow guiding member, comprising an elongated member having a proximal end and a distal end, and an elongated body extending between the proximal end and the distal end, wherein the elongated body comprises at least a section such that when the elongated body is cut at any position along the flow guiding direction within the section, only a pair of points furthest apart can be found on the outer periphery of the obtained cross-section (referred to as the total cross-section), referred to as a first point and a second point, respectively, the outer periphery of the total cross-section being divided by the first point and the second point into a first line and a second line connected end to end, the straight line segment connecting the first point and the second point being referred to as a dividing line, wherein the length of the first line is L1, and the length of the second line is L2, then the value of L1 / L2 is greater than 1 (preferably 1.01-1.5 or 1.03-1.2).

2. The flow guiding member according to claim 1, satisfying at least one (preferably all) of the following conditions: 1) The first line is a curve (preferably a smooth curve, more preferably a smooth curve composed of multiple circular arcs / elliptical arcs), and the second line is a curve (preferably a smooth curve, more preferably a smooth curve composed of multiple circular arcs / elliptical arcs) or a straight line. 2) The entire length of the dividing line lies within the total cross-section or on the outer periphery of the total cross-section. 3) The portion of the total cross-section surrounded by the dividing line and the first line is called the first cross-section, and the portion of the total cross-section surrounded by the dividing line and the second line is called the second cross-section. Let the area of ​​the first cross-section be A1 and the area of ​​the second cross-section be A2. Then the value of A1 / A2 (provided that neither the first line nor the second line is a straight line) is greater than 1 (preferably 1.1-21 or 2-9).

3. The flow guide member of claim 2, wherein the curve is a convex curve (such as a part of a circle or ellipse (especially a minor arc), preferably a quarter or less of a circular arc or elliptical arc) or a streamlined curve (preferably a combination of circular arcs and elliptical arcs and elliptical arcs).

4. The flow guiding component according to claim 1, wherein the first line and the second line are each composed of two circular arcs / elliptical arcs, the length ratio of the dividing line corresponding to the two circular arcs / elliptical arcs constituting the first line is a1 / a2 = 0.05-0.6 (preferably 0.1-0.4), and the length ratio of the dividing line corresponding to the two circular arcs / elliptical arcs constituting the second line is a1 / a2 = 0.05-0.6 (preferably 0.1-0.4).

5. The flow guide member of claim 1, wherein at the proximal end, the total cross-sectional area is 400-25000 mm². 2 At the distal end, the total cross-sectional area is 1-1500 mm. 2 .

6. The flow guide member according to claim 1, wherein at the proximal end, L1 = 60-600 mm (preferably 100-400 mm), and at the distal end, L1 = 3-150 mm (preferably 20-60 mm).

7. The flow guiding member of claim 1, wherein the first line and the second line intersect at the first point and the second point respectively, forming a closed shape.

8. The flow guide member according to claim 1, wherein the length of the elongated body is 50-400 mm (preferably 100-300 mm), and the length of the section is 30-100% (preferably 70-100%) of the length of the elongated body.

9. The flow guiding member of claim 1, wherein when the distal end of the elongated body is cut along the flow guiding direction, the obtained cross section is called the distal cross section, and when the proximal end of the elongated body is cut along the flow guiding direction, the obtained cross section is called the proximal cross section, and the length of the boundary line of the distal cross section is H1, and the length of the boundary line of the proximal cross section is H2, then H1 / H2 = 0.005-1 (preferably 0.05-0.5).

10. The flow guiding member according to claim 9, wherein H1 = 2-100 mm (preferably 15-50 mm) and H2 = 50-400 mm (preferably 80-300 mm).

11. The flow guiding member of claim 9, wherein when the elongated body is cut at any two positions between the distal end and the proximal end along the flow guiding direction, the two obtained cross sections are respectively referred to as the first sampling cross section and the second sampling cross section, wherein the first sampling cross section is closer to the proximal end than the second sampling cross section, and the length of the boundary line of the first sampling cross section is Hm, and the length of the boundary line of the second sampling cross section is Hn, then Hm≥Hn (preferably Hm>Hn).

12. The flow guide member of claim 1, wherein the length of the dividing line of the cross section of the elongated body gradually decreases continuously or intermittently from the proximal end to the distal end (preferably continuously and monotonically decreasing).

13. The flow guide member of claim 1, wherein the angle between the length direction of the elongated body and the dividing line is 30-90 degrees (preferably 60-90 degrees).

14. The flow guiding member of claim 1 further includes a columnar member, wherein the elongated member and the columnar member are connected to each other at the proximal end, such that the elongated member is arranged symmetrically or asymmetrically about the central axis of the columnar member on one side or both sides of the columnar member, or, when two or more elongated members are provided, the included angle between the length directions of two adjacent elongated members is greater than 0 degrees and not greater than 180 degrees (preferably 60-180 degrees, more preferably 90-150 degrees).

15. The flow guide member of claim 1, wherein when the direction of the central axis of the columnar member is perpendicular, the angle between the dividing line and the perpendicular direction is 0 to 30° (preferably 0 to 10°) or 0 to -30° (preferably 0 to -10°).

16. The flow guiding member of claim 1 further includes a sheet-like member, wherein the sheet-like member is connected to the columnar member such that the sheet-like member is arranged symmetrically or asymmetrically about one or both sides of the columnar member with respect to the central axis of the columnar member.

17. The flow guiding member of claim 16, wherein two or more of the sheet-like members and two or more of the elongated members are alternately arranged on the columnar member, preferably two adjacent elongated members are arranged symmetrically or asymmetrically on one or both sides of the sheet-like member with respect to the plane direction of one sheet-like member.

18. The flow guiding member of claim 16, wherein when the direction of the central axis of the columnar member is perpendicular, the angle between the planar direction of the sheet-like member and the perpendicular direction is 0-30 degrees (preferably 0-10 degrees).

19. The flow guide member of claim 16, wherein the projected shape of the sheet member is at least one selected from rectangle, triangle, trapezoid, semi-ellipse and irregular shape, preferably semi-ellipse.

20. The flow guiding member of claim 16, wherein the ratio of the projected area of ​​the sheet-like member to that of the elongated member is 0.05-0.

6.

21. The flow guiding member of claim 16, wherein the sheet-like member has a width of 5-100 mm, a height of 10-300 mm, and a thickness of 2-10 mm.

22. The flow guiding member of claim 14 further includes a connecting rod, wherein one or more of the columnar members are fixedly disposed on the connecting rod.

23. The flow guiding member of claim 22, wherein the spacing between the plurality of columnar members (based on the central axis) is 100-1000 mm (preferably 200-400 mm).

24. The flow guiding member of claim 22, wherein the angle between the central axis of the connecting rod and the central axis of the columnar member is 45-90 degrees (preferably about 90 degrees).

25. The flow guide member of claim 22, wherein a plurality of connecting rods are arranged in the same horizontal plane, and the horizontal projections of the spanwise fins on opposite sides of two adjacent connecting rods in the longitudinal direction are substantially parallel.

26. A fluidized bed reactor, comprising a shell and a flow guiding member disposed inside the shell, wherein the flow guiding member comprises the flow guiding member according to any one of claims 1-25.

27. The reactor of claim 26, wherein the flow guiding member is provided in multiple layers (e.g., 2-20 layers) along the central axis of the reactor, and the vertical spacing between each layer (based on the central axis of the connecting rod) is 0.1-0.25 times the diameter of the reactor.

28. The reactor of claim 26, wherein the central axes of the connecting rods of adjacent flow guide members form an angle of approximately 90 degrees.

29. The reactor of claim 26 further includes a gas distributor, wherein the lowest layer of the flow guiding member is disposed above the gas distributor, and the vertical distance between the gas distributor and the gas distributor (based on the central axis of the connecting rod) is 0.1-0.2 times the diameter of the reactor.

30. The reactor of claim 26, wherein multiple rows (e.g., 9-39 rows) of the flow guiding members are arranged in the same cross-section of the reactor, and the horizontal spacing between each row (based on the central axis of the connecting rod) is 0.025-0.1 times the diameter of the reactor.

31. The reactor of claim 26, wherein, when the pressure standard deviation Sd, calculated by the following formula, characterizes the intensity of pressure pulsations within the reactor, Sd ≤ 8 kPa (preferably ≤ 4 kPa). in, Sd represents the standard deviation of pressure at any measurement point; N represents the number of sampled data; Pi represents the transient pressure at any time. This represents the average pressure. P' represents the pressure fluctuation value.

32. A fluidized bed reaction method, comprising the step of carrying out a chemical reaction in the fluidized bed reactor according to any one of claims 26-31.

33. The reaction method of claim 32, wherein the chemical reaction is a cold hydrogenation reaction of silicon tetrachloride, an organosilicon synthesis reaction, or a hydrogenation reaction of nitrobenzene to aniline.

34. The reaction method of claim 32, wherein the reaction conditions for the cold hydrogenation reaction include: The reaction temperature is 450-620℃, the reaction pressure is 2.0-4.0MPaG, and the apparent linear velocity of the gas is 0.05-0.8m / s.

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