CN115364778A - Fluidized bed - Google Patents
Fluidized bed Download PDFInfo
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- CN115364778A CN115364778A CN202211017866.4A CN202211017866A CN115364778A CN 115364778 A CN115364778 A CN 115364778A CN 202211017866 A CN202211017866 A CN 202211017866A CN 115364778 A CN115364778 A CN 115364778A
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 78
- 238000005243 fluidization Methods 0.000 claims abstract description 43
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000010949 copper Substances 0.000 claims abstract description 19
- 229910052802 copper Inorganic materials 0.000 claims abstract description 19
- 230000007246 mechanism Effects 0.000 claims description 45
- 238000005507 spraying Methods 0.000 claims description 16
- 230000001133 acceleration Effects 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims 2
- 239000000376 reactant Substances 0.000 abstract description 10
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 38
- 239000011863 silicon-based powder Substances 0.000 description 38
- 239000012495 reaction gas Substances 0.000 description 12
- 238000009835 boiling Methods 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 230000008878 coupling Effects 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 4
- 238000005859 coupling reaction Methods 0.000 description 4
- 230000000149 penetrating effect Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 235000013312 flour Nutrition 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/32—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with introduction into the fluidised bed of more than one kind of moving particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a fluidized bed, which comprises an upper tube box, a reaction cylinder, a lower tube box, an upper tube plate, a first heat exchange tube, a feed inlet, an air inlet and a discharge tube, wherein the upper tube box, the reaction cylinder and the lower tube box are sequentially communicated from top to bottom; the fluidized bed also comprises a first copper pipe which is sleeved on the first heat exchange pipe and is positioned in the stable fluidization section of the dilute phase zone. The fluidized bed can greatly improve the reaction capability of reactants in a stable fluidized section of a dilute phase zone and improve the overall main reaction rate.
Description
Technical Field
The present invention relates to a fluidized bed.
Background
The existing fluidized bed is generally divided into a jet fluidization section, a dense-phase region boiling fluidization section, a dilute-phase region stable fluidization section and a settling section from bottom to top in sequence, wherein the jet fluidization section accounts for one fifth to one fourth of the total length, the dense-phase region boiling fluidization section accounts for one half to two thirds of the total length, the dilute-phase region stable fluidization section accounts for one fourth to one third of the total length, and the settling section accounts for one tenth to one fourth of the total length. Wherein, the reaction of the first stage and the second stage is more violent, and the reaction ratio of the third stage and the fourth stage is smaller.
The reason is that when the copper powder catalyst is injected at a high speed, the copper powder catalyst has large stacking density and large stacking density difference with the reactant silicon powder, the rising speed of the reactant silicon powder in the boiling fluidization section of the dense phase region is very low, the copper powder catalyst gradually separates and sinks in the boiling fluidization section of the dense phase region with a longer occupation ratio, so that the reaction density degree in the boiling fluidization section of the dense phase region is continuously reduced from bottom to top, the copper powder catalyst is difficult to reach the stable fluidization section of the dilute phase region, and the reaction of the reactant silicon powder in the stable fluidization section of the dilute phase region is basically stopped. The proportion of the dilute phase zone stable fluidization section in the total length is not low, so that the overall reaction efficiency of the fluidized bed is seriously influenced. The copper powder catalyst deposits on the lower part of the fluidized bed, which results in low main reaction rate of the reactant silicon powder, more side reactions and relatively low main reaction efficiency in unit volume.
Disclosure of Invention
The invention aims to provide a fluidized bed which can greatly improve the reaction capability of reactants in a stable fluidizing section of a dilute phase zone.
In order to achieve the purpose, the invention adopts the technical scheme that:
a fluidized bed comprises an upper tube box, a reaction cylinder, a lower tube box, an upper tube plate, a first heat exchange tube, a feed inlet, an air inlet and a discharge tube, wherein the upper tube box, the reaction cylinder and the lower tube box are sequentially communicated from top to bottom; the fluidized bed further comprises a first copper pipe which is sleeved on the first heat exchange pipe and is positioned in the dilute phase region stable fluidization section.
Preferably, the fluidized bed further comprises a second copper pipe which is annularly abutted to the periphery of the inner side of the reaction cylinder and is positioned in the dilute phase zone stable fluidization section.
Preferably, the first heat exchange tube has a plurality of tubes, or the first heat exchange tube has only one tube and is bent repeatedly along the up-down direction for a plurality of times;
the fluidized bed is still including connecting coupling assembling between the first heat exchange tube, coupling assembling includes a plurality of connecting pieces, every the connecting piece is all connected adjacently between the first heat exchange tube, the connecting piece layering is arranged, and is same height the quantity of connecting piece is less than and is used for connecting all adjacent first heat exchange tube the quantity of connecting piece.
Preferably, the fluidized bed further comprises a first circumferential acceleration mechanism located in the freeboard fluidization section;
the first circumferential accelerating mechanism comprises a first ring pipe, a first air inlet pipe and a plurality of first air outlet pipes, wherein the shaft axis of the first ring pipe extends along the vertical direction, the first air inlet pipe is communicated with the lower part of the first ring pipe, and the first air outlet pipes are uniformly arranged at intervals and communicated with the upper side part of the first ring pipe;
the first air outlet pipe is obliquely and upwards arranged along the air outlet direction, and the projection of the first air outlet pipe on the horizontal plane and the radial direction of the first ring pipe form an angle.
Preferably, the fluidized bed further comprises a spraying mechanism positioned in the lower pipe box, and a feeding pipe which is communicated with the feeding hole and upwards penetrates through the spraying mechanism;
the spraying mechanism comprises an air inlet ring pipe communicated with the air inlet, a porous plate positioned above the air inlet ring pipe and a nozzle arranged in the porous plate;
the axial lead of the air inlet ring pipe extends along the up-down direction, the top of the air inlet ring pipe is provided with a plurality of air outlet holes, the angle between the spraying direction of the nozzle and the axial lead of the reaction cylinder is alpha, wherein alpha is more than or equal to 0 degree and less than or equal to 5 degrees, and when alpha is more than 0 degree, the nozzle points inwards to the axial lead of the reaction cylinder along the spraying direction.
More preferably, the fluidized bed further comprises a second circumferential acceleration mechanism located above the injection mechanism;
the second circumferential accelerating mechanism comprises a second ring pipe, a second air inlet pipe and a plurality of second air outlet pipes, wherein the shaft axis of the second ring pipe extends along the vertical direction, the second air inlet pipe is communicated with the lower part of the second ring pipe, and the second air outlet pipes are uniformly arranged at intervals and communicated with the upper side part of the second ring pipe;
the second air outlet pipe is obliquely and upwards arranged along the air outlet direction, and the projection of the second air outlet pipe on the horizontal plane and the radial direction of the second ring pipe form an angle.
Preferably, the fluidized bed further comprises a second heat exchange tube wound on the periphery of the outer side of the reaction cylinder.
Preferably, the reaction cylinder further comprises a settling section connected above the dilute phase zone stable fluidization section.
Preferably, the fluidized bed further comprises a separation and recovery mechanism, the separation and recovery mechanism comprises a main separator communicated with the discharge pipe and a main return pipe, one end of the main return pipe is communicated with the main separator, and the other end of the main return pipe penetrates through the reaction cylinder.
More preferably, the separation and recovery mechanism further comprises a secondary separator communicated with the primary separator and a secondary return pipe, one end of the secondary return pipe is communicated with the secondary separator, and the other end of the secondary return pipe penetrates through the reaction cylinder.
Due to the application of the technical scheme, compared with the prior art, the invention has the following advantages: according to the fluidized bed, the first copper pipe is compounded on the outer side of the first heat exchange pipe and is positioned in the dilute phase zone stable fluidization section of the reaction cylinder, so that reactants rising to the height are catalyzed by the first copper pipe, the reaction capacity is greatly improved, and the overall reaction efficiency and the main reaction rate of the reactants in the fluidized bed are improved.
Drawings
FIG. 1 is a schematic diagram of a fluidized bed according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a first heat exchange tube;
FIG. 3 is a schematic cross-sectional view along AA of FIG. 2;
FIG. 4 is a schematic view of a connection structure of a first heat exchange tube and a connection assembly;
FIG. 5 is a schematic cross-sectional view taken along direction BB of FIG. 4;
FIG. 6 is a schematic structural view of a first circumferential acceleration mechanism;
FIG. 7 is a schematic cross-sectional view taken along the direction CC of FIG. 6;
fig. 8 is a schematic structural view of the spray mechanism of fig. 1.
Wherein: 1. an upper pipe box; 2. a reaction cylinder; 3. a lower pipe box; 4. an upper tube sheet; 5. a first heat exchange tube; 6. a feed inlet; 7. an air inlet; 8. a discharge pipe; 9. a first copper tube; 10. a connecting member; 11. a first circumferential acceleration mechanism; 111. a first grommet; 112. a first intake pipe; 113. a first air outlet pipe; 12. an injection mechanism; 121. an air inlet ring pipe; 122. a perforated plate; 123. a nozzle; 13. a feed pipe; 14. a second circumferential acceleration mechanism; 15. a second heat exchange tube; 16. a separation and recovery mechanism; 161. a main feed back pipe; 162. and a secondary feed back pipe.
Detailed Description
The technical solution of the present invention is further explained below with reference to the specific embodiments and the accompanying drawings.
In the following, only certain exemplary embodiments are briefly described. As those skilled in the art will recognize, the described embodiments may be modified in various different ways, all without departing from the spirit or scope of the embodiments of the invention. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.
In the description of the embodiments of the present invention, it should be understood that the terms "length", "inside", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience in describing the embodiments of the present invention and simplifying the description, but do not indicate or imply that the referred devices or elements must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the embodiments of the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the embodiments of the present invention, "a plurality" means two or more unless specifically limited otherwise.
In the embodiments of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," "fixed," and the like are to be construed broadly, e.g., as being fixedly connected, detachably connected, or integrated; the connection can be mechanical connection, electrical connection or communication; they may be directly connected or indirectly connected through intervening media, or may be connected through the use of two elements or the interaction of two elements. Specific meanings of the above terms in the embodiments of the present invention can be understood by those of ordinary skill in the art according to specific situations.
In embodiments of the invention, unless expressly stated or limited otherwise, the first feature "on" or "under" the second feature may comprise the first and second features being in direct contact, or the first and second features being in contact, not directly, but via another feature therebetween. Also, the first feature being "on," "above" and "over" the second feature includes the first feature being directly on and obliquely above the second feature, or merely indicating that the first feature is at a higher level than the second feature. "beneath," "under" and "beneath" a first feature includes the first feature being directly beneath and obliquely beneath the second feature, or simply indicating that the first feature is at a lesser elevation than the second feature.
The following disclosure provides many different embodiments or examples for implementing different configurations of embodiments of the invention. To simplify the disclosure of embodiments of the invention, the components and arrangements of specific examples are described below. Of course, they are merely examples and are not intended to limit embodiments of the invention. Furthermore, embodiments of the present invention may repeat reference numerals and/or letters in the various examples, such repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed.
Referring to fig. 1, the present embodiment provides a fluidized bed, which includes an upper tube box 1, a reaction barrel 2, a lower tube box 3, an upper tube plate 4 sealed between the upper tube box 1 and the reaction barrel 2, a first heat exchange tube 5 disposed in the reaction barrel 2, a feed inlet 6 and an air inlet 7 opened on the lower tube box 3, a discharge tube 8 with a lower end penetrating through the upper tube plate 4 and an upper end penetrating upward through the upper tube box 1, wherein two ends of the first heat exchange tube 5 respectively penetrate through the upper tube plate 4 and communicate with the upper tube box 1. The reaction cylinder 2 comprises a jetting fluidization section, a dense phase zone boiling fluidization section, a dilute phase zone stable fluidization section and a sedimentation section which are sequentially connected from bottom to top, the four sections are integrally formed, and only the corresponding reaction stages are different.
The fluidized bed is used for the reaction of reactant silicon powder and reaction gas under the high-temperature condition, and the reaction capability of the reactant silicon powder is improved through a copper powder catalyst. The feeding port 6 is used for introducing reaction gas, silicon powder and copper powder, the silicon powder and the copper powder are driven to rise in the reaction cylinder 2 by the reaction gas, and the gas inlet 7 is only used for introducing the reaction gas. During actual reaction, reaction gas and silicon powder are firstly introduced into the feeding port 6, and copper powder is simultaneously introduced when the temperature reaches the standard.
Referring to fig. 2-3, in this embodiment, the fluidized bed further includes a first copper pipe 9 sleeved on the first heat exchange pipe 5 and located in the dilute phase zone stable fluidization section, the first copper pipe 9 is located at the middle upper position of the first heat exchange pipe 5, and the first heat exchange pipe 5 is a carbon steel pipe. The length of the first copper pipe 9 is the same as that of the dilute phase zone stable fluidization segment, the dilute phase zone stable fluidization segment accounts for about 35% of the total length of the reaction cylinder 2, and the thickness of the first copper pipe 9 is about 2 mm.
Because the stacking density difference between the copper powder and the silicon powder is large, the copper powder serving as a catalyst is easy to sink at the lower part of a fluidized bed during fluidization, is difficult to rise to reach a dilute phase region stable fluidization section, and only plays a role in greatly improving the reaction capacity of the silicon powder in a jet fluidization section and a dense phase region boiling fluidization section. The silicon powder basically loses reaction capability in a stable fluidization section and a stable sedimentation section of a dilute phase zone, so that the reaction rate of main reaction in the fluidized bed is low, side reactions are relatively more, and the main reaction efficiency in unit volume of the fluidized bed is influenced.
Through compounding a layer of first copper pipe 9 outside the first heat exchange tube 5, when silica flour rises to the dilute phase zone stabilized fluidization section, this first copper pipe 9 can play catalytic reaction's effect, improves the reaction ability of silica flour at the dilute phase zone stabilized fluidization section by a wide margin to improve the holistic reaction efficiency of fluidized bed and reaction ability.
To further increase the reaction capacity, the height of the first copper tube 9 may extend up into the settling section to increase the reaction capacity of the silicon powder in the settling section.
In another embodiment, the fluidized bed further comprises a second copper pipe (not shown) surrounding the inner periphery of the reaction cylinder 2 and located in the dilute-phase zone stable fluidization segment. Through the arrangement, the contact area of the silicon powder and the copper powder in the stable fluidization section of the dilute phase zone is increased, and the reaction capacity of the silicon powder in the stable fluidization section of the dilute phase zone is further improved. Obviously, the height of the second copper pipe can also extend upwards into the settling section to improve the reaction capacity of the silicon powder in the settling section.
In this embodiment, only one first heat exchange tube 5 is bent in a reciprocating manner several times in the up-down direction, that is, the first heat exchange tube 5 is formed by sequentially communicating a plurality of U-shaped tubes, and two ends of the first heat exchange tube 5 respectively penetrate through the upper tube plate 4 upwards and upwards penetrate out of the upper tube box 1 for inputting and outputting heat conducting oil to absorb heat emitted by the reaction.
In another embodiment, the first heat exchange tube 5 is composed of a plurality of U-shaped tubes, and both ends of each U-shaped tube respectively penetrate upward through the upper tube plate 4 and upward out of the upper tube box 1 for inputting and outputting heat conducting oil to absorb heat released by the reaction.
The fluidized bed further includes a connection assembly connected between the first heat exchange tubes 5, the connection assembly including a plurality of connection members 10, each connection member 10 being connected between the adjacent first heat exchange tubes 5. The connecting pieces 10 are arranged in layers, the number of the connecting pieces 10 with the same height is less than that of the connecting pieces 10 used for connecting all the adjacent first heat exchange tubes 5, and the adjacent connecting pieces 10 are staggered and have different heights.
Referring to fig. 4-5, the connection assembly is comprised of a plurality of connection members 10, the plurality of connection members 10 being adapted to form a full support structure for the first heat exchange tube 5. In the present embodiment, the first heat exchange tube 5 is integrally supported in four layers. Fig. 5 (1) corresponds to the uppermost first layer, fig. 5 (2) corresponds to the second layer lower than the first layer only, fig. 5 (3) corresponds to the third layer lower than the second layer, and fig. 5 (4) corresponds to the lowermost fourth layer. Obviously, the connecting components can have multiple groups and are arranged at intervals along the up-down direction according to the length of the reaction cylinder 2.
The support structure has the advantages that the connecting pieces 10 are layered, the number of the connecting pieces 10 with the same height is greatly reduced on the basis of not influencing the connecting strength between the first heat exchange tubes 5, the upward flowing permeability of silicon powder is improved, the obstruction of the connecting components to the flowing of the silicon powder is reduced to the minimum, the uniformity of a temperature field in the reaction cylinder 2 can be improved, and the occupation ratio of main reaction is improved.
In the prior art, all the connecting pieces 10 in one group of connecting components are located at the same height of the same layer, so that the movement of fluidized silicon powder is hindered, the fluidized state is disturbed, and the uniformity of a temperature field in the reaction cylinder 2 is poor. The fluidized bed has the diameter of 4m or more, the total height of 15 m or more and the capacity of 25W ton/year or more. The fluidized bed is higher, and the number of piles that coupling assembling is piled up along upper and lower direction is more, adopts coupling assembling's structure in this application, and the permeability that the silica powder upflow is better.
Referring to fig. 6-7, the fluidized bed further includes a first circumferential acceleration mechanism 11 located in the freeboard fluidization section. In this embodiment, the first circumferential accelerating mechanism 11 includes a first collar 111 extending along a vertical direction, a first air inlet pipe 112 communicating with a lower portion of the first collar 111, and a plurality of first air outlet pipes 113 communicating with an upper portion of the first collar 111 and arranged at regular intervals. The first air outlet pipe 113 is obliquely arranged upwards along the air outlet direction, and the projection of the first air outlet pipe 113 on the horizontal plane along the vertical direction and the radial direction of the first ring pipe 111 form an angle.
With this arrangement, the silicon powder output from the first gas outlet pipe 113 can not only rise, but also rise around the first heat exchange pipe 5, i.e., spirally. The contact time and the contact area of the silicon powder and the first copper pipe 9 are increased, and the reaction efficiency of the silicon powder in the stable fluidization section of the dilute phase zone is further improved.
Referring to fig. 8, the fluidized bed further includes a spraying mechanism 12 in the lower tube box 3, and a feeding pipe 13 communicating with the feeding port 6 and upwardly penetrating the spraying mechanism 12. The injection mechanism 12 comprises an inlet collar 121 communicating with the air inlet 7, a perforated plate 122 located above the inlet collar 121, and nozzles 123 provided in the perforated plate 122, with the feed pipe 13 passing upwardly through the inlet collar 121 and the perforated plate 122.
In this embodiment, the axis of the air inlet ring pipe 121 extends in the vertical direction, the top of the air inlet ring pipe 121 is provided with a plurality of air outlets, and the perforated plate 122 is provided with a plurality of through holes for installing the nozzles 123 in a one-to-one correspondence. The angle between the spraying direction of the nozzle 123 and the axial lead of the reaction cylinder 2 is alpha, wherein alpha is more than or equal to 0 degree and less than or equal to 5 degrees, and when alpha is more than 0 degree, the nozzle 123 points inwards to the axial lead of the reaction cylinder 2 along the spraying direction.
Through the arrangement, the problem that silicon powder flowing at high speed intensively impacts the first heat exchange tube 5 on the inner side upwards to cause easy abrasion and short service life can be avoided.
Referring to fig. 1, the fluidized bed further comprises a second circumferential accelerating means 14 located above the spraying means 12. In this embodiment, the second circumferential acceleration mechanism 14 includes a second circular pipe having an axis extending in a vertical direction, a second air inlet pipe communicating with a lower portion of the second circular pipe, and a plurality of second air outlet pipes evenly spaced and communicating with an upper side portion of the second circular pipe. The second air outlet pipe is obliquely and upwards arranged along the air outlet direction, and the projection of the second air outlet pipe on the horizontal plane along the vertical direction and the radial direction of the second ring pipe form an angle with each other. The second circumferential acceleration mechanism 14 has the same structure as the first circumferential acceleration mechanism 11, and is not shown in detail.
With this arrangement, the silicon powder output from the second outlet pipe can not only rise, but also rise spirally around the inner peripheral portion of the reaction cylinder 2. The convection heat exchanger coefficient between the silicon powder and the first heat exchange tube 5 is strengthened, and the reaction efficiency of the silicon powder is improved.
Referring to fig. 1, the fluidized bed further includes a second heat exchange tube 15 wound around the outer periphery of the reaction cylinder 2, and the second heat exchange tube 15 is also used for inputting and outputting heat conducting oil to absorb heat released by the reaction.
The fluidized bed further comprises a separation and recovery mechanism 16, wherein the separation and recovery mechanism 16 comprises a main separator (not shown in the figure) communicated with the discharge pipe 8 and a main return pipe 161 with one end communicated with the main separator, and the other end of the main return pipe 161 is arranged in the reaction cylinder 2 in a penetrating way. In this embodiment, the upper end of the main feed back pipe 161 is communicated with the main separator, and the lower end of the main feed back pipe 161 penetrates into the reaction cylinder 2 and is slightly higher than the second circumferential acceleration mechanism 14.
In the present embodiment, the separation and recovery mechanism 16 further includes a secondary separator (not shown in the figure) communicating with the primary separator for performing secondary separation, and a secondary return pipe 162 having an upper end communicating with the secondary separator, wherein a lower end of the secondary return pipe 162 penetrates into the reaction cylinder 2 and is located between a lower end of the primary return pipe 161 and the second circumferential acceleration mechanism 14.
By adopting the fluidized bed of the embodiment, the heat transfer efficiency is improved by 10-25%, the overall reaction efficiency is improved by 13-20%, the start cycle is improved from about 35 days to about 49 days, and the cost is saved by about 15% for the same production capacity.
The following specifically explains the working process of the present embodiment:
part of reaction gas carrying silicon powder and copper powder is input from the feed inlet 6 and output from the upper end of the feed pipe 13, and the other part of reaction gas is input from the gas inlet 7, and the silicon powder and the copper powder output from the feed pipe 13 are upwards sprayed by the spraying mechanism 12 and enter the second circumferential acceleration mechanism 14 to be output;
the silicon powder, copper powder and reaction gas output by the second circumferential acceleration mechanism 14 collide with the silicon powder refluxed in the secondary material return pipe 162 and move upward together, and the silicon powder and the reaction gas rise while reacting under the catalysis of the copper powder and then collide with the silicon powder refluxed by the main material return pipe 161 and react; the heat in the reaction cylinder 2 is led out through the first heat exchange tube 5 and the second heat exchange tube 15;
when silicon powder, copper powder and reaction gas sequentially pass through the jet fluidization section and the dense-phase region boiling fluidization section upwards and enter the dilute-phase region stable fluidization section, the copper powder is deposited downwards, the silicon powder and the reaction gas spirally rise through the first circumferential accelerating mechanism 11, and the reaction capacity and the reaction efficiency of the silicon powder are improved through the first copper pipe 9 on the outer side of the first heat exchange pipe 5;
finally, silicon powder, reaction gas and reaction products are output from the discharge pipe 8, the silicon powder subjected to primary separation by the primary separator enters the primary return pipe 161, and the silicon powder obtained after secondary separation by the secondary separator enters the secondary return pipe 162.
The above-mentioned embodiments are merely illustrative of the technical idea and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the scope of the present invention, and all equivalent changes or modifications made according to the spirit of the present invention should be covered in the scope of the present invention.
Claims (10)
1. A fluidized bed comprises an upper tube box, a reaction cylinder, a lower tube box, an upper tube plate, a first heat exchange tube, a feed inlet, an air inlet and a discharge tube, wherein the upper tube box, the reaction cylinder and the lower tube box are sequentially communicated from top to bottom; the method is characterized in that:
the fluidized bed further comprises a first copper pipe which is sleeved on the first heat exchange pipe and is positioned in the dilute phase region stable fluidization section.
2. The fluid bed according to claim 1, characterized in that: the fluidized bed also comprises a second copper pipe which is annularly propped against the periphery of the inner side of the reaction cylinder and is positioned in the dilute phase zone stable fluidization section.
3. The fluid bed according to claim 1, characterized in that: the first heat exchange tube is provided with a plurality of first heat exchange tubes, or only one first heat exchange tube is provided and is bent repeatedly along the up-down direction for a plurality of times;
the fluidized bed is characterized by further comprising a connecting assembly connected between the first heat exchange tubes, wherein the connecting assembly comprises a plurality of connecting pieces, each connecting piece is connected between the adjacent first heat exchange tubes, the connecting pieces are arranged in a layered mode, and the number of the connecting pieces at the same height is less than that of the connecting pieces used for connecting all the adjacent first heat exchange tubes.
4. The fluidized bed according to claim 1, characterized in that: the fluidized bed further comprises a first circumferential acceleration mechanism located in the dilute phase zone stable fluidization section;
the first circumferential accelerating mechanism comprises a first ring pipe, a first air inlet pipe and a plurality of first air outlet pipes, wherein the shaft axis of the first ring pipe extends along the vertical direction, the first air inlet pipe is communicated with the lower part of the first ring pipe, and the first air outlet pipes are uniformly arranged at intervals and communicated with the upper side part of the first ring pipe;
the first air outlet pipe is obliquely and upwards arranged along the air outlet direction, and the projection of the first air outlet pipe on the horizontal plane and the radial direction of the first ring pipe form an angle.
5. The fluidized bed according to claim 1, characterized in that: the fluidized bed also comprises a spraying mechanism positioned in the lower pipe box, and a feeding pipe which is communicated with the feeding hole and upwards penetrates through the spraying mechanism;
the spraying mechanism comprises an air inlet ring pipe communicated with the air inlet, a porous plate positioned above the air inlet ring pipe and a nozzle arranged in the porous plate;
the axial lead of the air inlet ring pipe extends along the up-down direction, the top of the air inlet ring pipe is provided with a plurality of air outlet holes, the angle between the spraying direction of the nozzle and the axial lead of the reaction cylinder is alpha, wherein alpha is more than or equal to 0 degree and less than or equal to 5 degrees, and when alpha is more than 0 degree, the nozzle points inwards to the axial lead of the reaction cylinder along the spraying direction.
6. The fluidized bed of claim 5, wherein: the fluidized bed further comprises a second circumferential acceleration mechanism located above the injection mechanism;
the second circumferential accelerating mechanism comprises a second ring pipe, a second air inlet pipe and a plurality of second air outlet pipes, wherein the shaft axis of the second ring pipe extends along the vertical direction, the second air inlet pipe is communicated with the lower part of the second ring pipe, and the second air outlet pipes are uniformly arranged at intervals and communicated with the upper side part of the second ring pipe;
the second air outlet pipe is obliquely and upwards arranged along the air outlet direction, and the projection of the second air outlet pipe on the horizontal plane and the radial direction of the second ring pipe form an angle.
7. The fluidized bed according to claim 1, characterized in that: the fluidized bed also comprises a second heat exchange tube wound on the periphery of the outer side of the reaction cylinder.
8. The fluidized bed according to claim 1, characterized in that: the reaction cylinder also comprises a settling section connected above the dilute phase zone stable fluidization section.
9. The fluidized bed according to claim 1, characterized in that: the fluidized bed further comprises a separation and recovery mechanism, the separation and recovery mechanism comprises a main separator communicated with the discharge pipe and a main material return pipe, one end of the main material return pipe is communicated with the main separator, and the other end of the main material return pipe penetrates through the reaction cylinder.
10. The fluidized bed of claim 9, wherein: the separation and recovery mechanism further comprises a secondary separator communicated with the main separator and a secondary return pipe, one end of the secondary return pipe is communicated with the secondary separator, and the other end of the secondary return pipe penetrates through the reaction cylinder.
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| KR20070069622A (en) * | 2005-12-28 | 2007-07-03 | 주식회사 엘지화학 | Fluidized bed reactor |
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