CN115364778B - Fluidized bed - Google Patents
Fluidized bed Download PDFInfo
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- CN115364778B CN115364778B CN202211017866.4A CN202211017866A CN115364778B CN 115364778 B CN115364778 B CN 115364778B CN 202211017866 A CN202211017866 A CN 202211017866A CN 115364778 B CN115364778 B CN 115364778B
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 77
- 238000005243 fluidization Methods 0.000 claims abstract description 42
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000010949 copper Substances 0.000 claims abstract description 20
- 229910052802 copper Inorganic materials 0.000 claims abstract description 20
- 230000007246 mechanism Effects 0.000 claims description 47
- 230000001133 acceleration Effects 0.000 claims description 22
- 238000002347 injection Methods 0.000 claims description 13
- 239000007924 injection Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 10
- 230000000149 penetrating effect Effects 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 7
- 230000002093 peripheral effect Effects 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 2
- 239000000376 reactant Substances 0.000 abstract description 9
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 36
- 239000011863 silicon-based powder Substances 0.000 description 36
- 239000012495 reaction gas Substances 0.000 description 11
- 238000009835 boiling Methods 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 4
- 235000013312 flour Nutrition 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
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- 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, a discharge tube, at least one end of the first heat exchange tube passes through the upper tube plate and is communicated with the upper tube box, wherein the upper tube plate is sealed between the upper tube box and the reaction cylinder; the fluidized bed further comprises a first copper pipe sleeved on the first heat exchange pipe and positioned in the dilute phase zone stable fluidization section. The fluidized bed can greatly improve the reaction capacity of reactants in the stable fluidization section of the 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 zone boiling fluidization section, a dilute-phase zone stable fluidization section and a sedimentation 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 zone boiling fluidization section accounts for one half to two thirds of the total length, the dilute-phase zone stable fluidization section accounts for one fourth to one third of the total length, and the sedimentation section accounts for one tenth to one fourth of the total length. Wherein the reaction of the first section and the second section is relatively intense, and the reaction of the third section and the fourth section occupies relatively small area.
The copper powder catalyst is gradually separated and sunk in the boiling fluidization section of the dense phase area, so that the reaction density in the boiling fluidization section of the dense phase area is continuously reduced from bottom to top, the copper powder catalyst is difficult to reach the stable fluidization section of the dilute phase area, and the reaction of the reactant silicon powder in the stable fluidization section of the dilute phase area is basically stagnant. The overall reaction efficiency of the fluidized bed is severely affected by the fact that the dilute phase zone stabilizing fluidization section has a low overall length. Copper powder catalyst is deposited at the lower part of the fluidized bed, so that the main reaction rate of reactant silicon powder is low, side reactions are more, and the main reaction efficiency in unit volume is relatively low.
Disclosure of Invention
The invention aims to provide a fluidized bed which can greatly improve the reaction capacity of reactants in a stable fluidization section of a dilute phase zone.
In order to achieve the above purpose, the invention adopts the following technical scheme:
the fluidized bed comprises an upper pipe box, a reaction cylinder, a lower pipe box, an upper pipe plate, a first heat exchange pipe, a feed inlet, an air inlet and a discharge pipe, wherein the upper pipe box, the reaction cylinder and the lower pipe box are sequentially communicated from top to bottom; the fluidized bed further comprises a first copper pipe sleeved on the first heat exchange pipe and positioned in the dilute phase zone stable fluidization section.
Preferably, the fluidized bed further comprises a second copper tube positioned in the dilute phase zone stable fluidization section and looped against the inner peripheral portion of the reaction cylinder.
Preferably, the first heat exchange tube has a plurality of pieces, or the first heat exchange tube has only one piece and is bent repeatedly along the up-down direction for several times;
the fluidized bed further comprises a connecting assembly connected between the first heat exchange tubes, 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 smaller than that of the connecting pieces used for connecting all the adjacent first heat exchange tubes.
Preferably, the fluidized bed further comprises a first circumferential acceleration mechanism located in the dilute phase zone stationary fluidization section;
the first circumferential acceleration mechanism comprises a first annular pipe, a first air inlet pipe and a plurality of first air outlet pipes, wherein the axial lead of the first annular pipe extends along the up-down direction, the first air inlet pipe is communicated with the lower part of the first annular pipe, and the first air outlet pipes are communicated with the upper side part of the first annular pipe in a uniformly arranged mode at intervals;
the first air outlet pipe is obliquely 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 annular pipe are mutually angled.
Preferably, the fluidized bed further comprises a spraying mechanism in the lower pipe box, and a feeding pipe which is communicated with the feeding hole and passes through the spraying mechanism upwards;
the injection 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, a plurality of air outlet holes are formed in the top of the air inlet ring pipe, the angle between the injection 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 injection direction.
More preferably, the fluidized bed further comprises a second circumferential acceleration mechanism located above the injection mechanism;
the second circumferential acceleration mechanism comprises a second annular pipe, a second air inlet pipe and a plurality of second air outlet pipes, wherein the axial lead of the second annular pipe extends along the up-down direction, the second air inlet pipe is communicated with the lower part of the second annular pipe, and the second air outlet pipes are communicated with the upper side part of the second annular pipe in a uniformly arranged mode at intervals;
the second air outlet pipe is obliquely 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 circular pipe are mutually angled.
Preferably, the fluidized bed further comprises a second heat exchange tube wound around the outer peripheral portion of the reaction cylinder.
Preferably, the reaction drum 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 feed back pipe with one end communicated with the main separator, and the other end of the main feed back pipe is arranged in the reaction cylinder in a penetrating manner.
More preferably, the separation and recovery mechanism further comprises a secondary separator communicated with the primary separator, and a secondary feed back pipe with one end communicated with the secondary separator, wherein the other end of the secondary feed back 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 the first copper pipe 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 view 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 taken along the direction AA in FIG. 2;
FIG. 4 is a schematic diagram of a connection structure of the first heat exchange tube and the connection assembly;
FIG. 5 is a schematic cross-sectional view of FIG. 4 taken along BB;
FIG. 6 is a schematic structural view of a first circumferential acceleration mechanism;
FIG. 7 is a schematic cross-sectional view of FIG. 6 taken along the direction CC;
fig. 8 is a schematic view of the injection mechanism of fig. 1.
Wherein: 1. a pipe feeding 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 piece; 11. a first circumferential acceleration mechanism; 111. a first collar; 112. a first air inlet pipe; 113. a first air outlet pipe; 12. a spraying mechanism; 121. an air inlet ring pipe; 122. a porous 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 scheme of the invention is further described below with reference to specific embodiments and drawings.
Hereinafter, only certain exemplary embodiments are briefly described. As will be recognized by those of skill in the pertinent art, the described embodiments may be modified in numerous different ways without departing from the spirit or scope of the embodiments of the present 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 orientation or positional relationship indicated by the terms "length", "inner", etc. are based on the orientation or positional relationship shown in the drawings, and are merely for convenience in describing the embodiments of the present invention and simplifying the description, and are not indicative or implying that the apparatus or element in question must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the embodiments of the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the embodiments of the present invention, the meaning of "plurality" is two or more, unless explicitly defined otherwise.
In the embodiments of the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured" and the like are to be construed broadly and include, for example, either permanently connected, removably connected, or integrally formed; the device can be mechanically connected, electrically connected and communicated; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the embodiments of the present invention will be understood by those of ordinary skill in the art according to specific circumstances.
In embodiments of the invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, or may include both the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
The following disclosure provides many different implementations, or examples, for implementing different configurations of embodiments of the invention. In order to simplify the disclosure of embodiments of the present invention, components and arrangements of specific examples are described below. Of course, they are merely examples and are not intended to limit embodiments of the present invention. Furthermore, embodiments of the present invention may repeat reference numerals and/or letters in the various examples, which are for the purpose of brevity and clarity, and which do not themselves indicate the relationship between the various embodiments and/or arrangements discussed.
Referring to fig. 1, this embodiment provides a fluidized bed, which includes an upper tube box 1, a reaction tube 2, a lower tube box 3, an upper tube plate 4 sealed between the upper tube box 1 and the reaction tube 2, a first heat exchange tube 5 arranged in the reaction tube 2, a feed inlet 6 and an air inlet 7 arranged 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 out of the upper tube box 1, and two ends of the first heat exchange tube 5 penetrating through the upper tube plate 4 and being communicated with the upper tube box 1. The reaction cylinder 2 comprises a jet 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, and 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 reactant gas at high temperature, and the reaction capacity of the reactant silicon powder is improved through the copper powder catalyst. Wherein, the feed inlet 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 air inlet 7 is only used for introducing the reaction gas. During actual reaction, the reaction gas and the silicon powder are firstly introduced into the feed inlet 6, and then copper powder is simultaneously introduced after the temperature reaches the standard.
Referring to fig. 2-3, in this embodiment, the fluidized bed further includes a first copper tube 9 sleeved on the first heat exchange tube 5 and located in the stable fluidized section of the dilute phase zone, the first copper tube 9 is located at a middle upper position of the first heat exchange tube 5, and the first heat exchange tube 5 is a carbon steel tube. The length of the first copper pipe 9 is the same as that of the dilute phase zone stable fluidization section, the dilute phase zone stable fluidization section 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 bulk density difference between copper powder and silicon powder is large, copper powder serving as a catalyst tends to be easy to sink at the lower part of a fluidized bed during fluidization, is difficult to rise to reach a stable fluidization section of a dilute phase zone, and only plays a role in greatly improving the reaction capacity of silicon powder in a jet fluidization section and a boiling fluidization section of a dense phase zone. The silicon powder basically loses the reaction capability in the dilute phase zone stable fluidization section and sedimentation section, so that the reaction rate of the main reaction in the fluidized bed is low, and the side reaction is relatively more, thereby influencing the main reaction efficiency in the volume of the fluidized bed unit.
Through compounding one deck first copper pipe 9 in the outside of first heat exchange tube 5, when the silica flour rises to the stable fluidization section of dilute phase district, this first copper pipe 9 can play catalytic reaction's effect, improves the reaction capacity of silica flour in the stable fluidization section of dilute phase district by a wide margin to the holistic reaction efficiency and the reaction capacity of fluidized bed improve.
To further increase the reaction capacity, the height of the first copper tube 9 may be extended 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 tube (not shown) positioned in the dilute phase zone stable fluidization section and looped against the inner periphery of the reaction drum 2. By the arrangement, the contact area of the silicon powder and the copper powder in the dilute phase zone stable fluidization section is increased, and the reaction capacity of the silicon powder in the dilute phase zone stable fluidization section is further improved. Obviously, the height of the second copper tube can also extend upwards into the settling section to improve the reactivity of the silicon powder in the settling section.
In this embodiment, only one first heat exchange tube 5 is bent reciprocally along the up-down direction for several times, that is, the first heat exchange tube 5 is formed by sequentially connecting a plurality of U-shaped tubes, and two ends of the first heat exchange tube 5 respectively pass through the upper tube plate 4 and pass through the upper tube box 1 upwards for inputting and outputting heat conduction oil to absorb heat released by the reaction.
In another embodiment, the first heat exchange tube 5 is composed of a plurality of U-shaped tubes, and two ends of each U-shaped tube respectively pass through the upper tube plate 4 and pass out of the upper tube box 1, so as to input and output heat conduction oil to absorb heat released by the reaction.
The fluidized bed further comprises a connection assembly connected between the first heat exchange tubes 5, the connection assembly comprising a plurality of connection members 10, each connection member 10 being connected between adjacent first heat exchange tubes 5. The connection members 10 are arranged in layers, the number of connection members 10 of the same height is smaller than the number of connection members 10 for connecting all the adjacent first heat exchange tubes 5, the adjacent connection members 10 are staggered from each other, and the heights are different.
Referring to fig. 4 to 5, the connection assembly is composed of a plurality of connection members 10, and the plurality of connection members 10 are used to form a full support structure for the first heat exchange tube 5. In the present embodiment, the overall support of the first heat exchange tube 5 is achieved 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 connection components can be multiple groups along with the different lengths of the reaction cylinders 2, and the connection components are arranged at intervals along the up-down direction.
The support structure has the advantages that the connecting pieces 10 are layered, the number of the connecting pieces 10 at the same height is greatly reduced on the basis that the connecting strength between the first heat exchange tubes 5 is not affected, the permeability of silicon powder flowing upwards is improved, the obstruction of the connecting assembly to the silicon powder flowing 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 a group of connecting assemblies are positioned at the same height of the same layer, so that the movement of the fluidized silicon powder is hindered, the fluidized state is disturbed, and the uniformity of the temperature field in the reaction cylinder 2 is poor. The fluidized bed has a diameter of 4m or more, a total height of 15 m or more and a capacity of 25W ton/year or more. The higher the height of the fluidized bed, the more the number of layers that the coupling assembling stacked along the upper and lower direction, adopts coupling assembling's structure in this application, and the permeability that silica flour upwards flowed is better.
Referring to fig. 6-7, the fluidized bed further comprises a first circumferential acceleration mechanism 11 located in the stationary fluidization section of the dilute phase zone. In the present embodiment, the first circumferential acceleration mechanism 11 includes a first collar 111 having an axis extending in the up-down direction, a first air inlet pipe 112 communicating with the lower portion of the first collar 111, and a plurality of first air outlet pipes 113 communicating with the upper side portion of the first collar 111 at regular intervals. The first air outlet pipe 113 is arranged obliquely 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 annular pipe 111 are mutually angled.
By this arrangement, the silicon powder output from the first air outlet pipe 113 can not only rise, but also be looped around the first heat exchange pipe 5, i.e., spirally rise. 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 region is further improved.
Referring to fig. 8, the fluidized bed further comprises a spraying mechanism 12 in the lower tube box 3, and a feed tube 13 communicating with the feed port 6 and passing upward through the spraying mechanism 12. The injection mechanism 12 includes an air intake collar 121 communicating with the air intake 7, a porous plate 122 located above the air intake collar 121, nozzles 123 provided in the porous plate 122, and a feed pipe 13 passing upward through the air intake collar 121 and the porous plate 122.
In this embodiment, the axis of the air inlet pipe 121 extends in the vertical direction, a plurality of air outlet holes are formed at the top of the air inlet pipe 121, and a plurality of through holes for installing the nozzles 123 are formed in the porous plate 122. The angle between the injection direction of the nozzle 123 and the axis of the reaction cylinder 2 is alpha, wherein alpha is more than or equal to 0 DEG and less than or equal to 5 DEG, and when alpha is more than 0 DEG, the nozzle 123 is directed inwards along the injection direction toward the axis of the reaction cylinder 2.
By this arrangement, the problem that the silicon powder flowing at a high speed intensively impacts the first heat exchange tube 5 on the inner side, resulting in easy wear and a short life can be avoided.
Referring to fig. 1, the fluidized bed further includes a second circumferential acceleration mechanism 14 located above the injection mechanism 12. In this embodiment, the second circumferential acceleration mechanism 14 includes a second collar having an axis extending in the up-down direction, a second air inlet pipe connected to the lower portion of the second collar, and a plurality of second air outlet pipes connected to the upper portion of the second collar in a uniformly spaced arrangement. The second outlet pipe is arranged obliquely upwards along the air outlet direction, and the projection of the second outlet pipe on the horizontal plane along the vertical direction forms an angle with the radial direction of the second annular pipe. The structure of the second circumferential acceleration mechanism 14 is the same as that of the first circumferential acceleration mechanism 11, and is not shown in detail.
By this arrangement, the silicon powder output from the second gas outlet pipe can not only rise, but also turn around the inner peripheral portion of the reaction tube 2, i.e., rise helically. The convection heat exchanger coefficient between the silicon powder and the first heat exchange tube 5 is enhanced, 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 circumference of the reaction vessel 2, and the second heat exchange tube 15 is also used for inputting and outputting heat transfer oil to absorb heat released from 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 feed back pipe 161 with one end communicated with the main separator, and the other end of the main feed back pipe 161 penetrates into the reaction cylinder 2. In this embodiment, the upper end of the main feed back pipe 161 communicates 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) communicating with the primary separator for secondary separation, and a secondary feed back pipe 162 having an upper end communicating with the secondary separator, the lower end of the secondary feed back pipe 162 penetrating into the reaction cylinder 2 and being located between the lower end of the primary feed back pipe 161 and the second circumferential acceleration mechanism 14.
By adopting the fluidized bed, the heat transfer efficiency is improved by 10-25%, the overall reaction efficiency is improved by 13-20%, the driving period is improved from about 35 days to about 49 days, and the same productivity is saved by about 15%.
The working procedure of this embodiment is specifically described below:
part of reaction gas carrying silicon powder and copper powder is input from a feed port 6, is output from the upper end of a feed pipe 13, and the other part of reaction gas is input from an air inlet 7, and the silicon powder and copper powder output from the feed pipe 13 are ejected upwards through an ejection mechanism 12 so as to enter a second circumferential acceleration mechanism 14 and then are output;
the silicon powder, copper powder and reaction gas output by the second circumferential acceleration mechanism 14 collide with the silicon powder reflowed in the secondary feedback pipe 162 and move upwards together, and the silicon powder and the reaction gas react while rising under the catalysis of the copper powder and collide with the silicon powder reflowed in the main feedback pipe 161 and react; heat in the reaction cylinder 2 is conducted out through the first heat exchange tube 5 and the second heat exchange tube 15;
when silicon powder, copper powder and reaction gas pass through the jet fluidization section and the dense-phase zone boiling fluidization section in turn upwards and enter the dilute-phase zone stable fluidization section, copper powder is deposited downwards, the silicon powder and the reaction gas are spirally lifted through the first circumferential acceleration mechanism 11, and the reaction capacity and the reaction efficiency of the silicon powder are improved through the first copper pipe 9 at the outer side of the first heat exchange pipe 5;
finally, the silicon powder, the reaction gas and the reaction product are output from the discharging pipe 8, the silicon powder subjected to primary separation by the primary separator enters the primary return pipe 161, and the silicon powder subjected to secondary separation by the secondary separator enters the secondary return pipe 162.
The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and to implement the same, but are not intended 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 included in the scope of the present invention.
Claims (8)
1. The fluidized bed comprises an upper pipe box, a reaction cylinder, a lower pipe box, an upper pipe plate, a first heat exchange pipe, a feed inlet, an air inlet and a discharge pipe, wherein the upper pipe box, the reaction cylinder and the lower pipe box are sequentially communicated from top to bottom; the method is characterized in that:
the fluidized bed further comprises a first copper pipe sleeved on the first heat exchange pipe and positioned in the dilute phase zone stable fluidization section; the fluidized bed further comprises a second copper pipe which is abutted against the inner peripheral part of the reaction cylinder and is positioned in the dilute phase zone stable fluidization section;
the first heat exchange tubes are provided with a plurality of pieces, or only one piece of first heat exchange tube is provided and is bent repeatedly along the up-down direction for a plurality of times;
the fluidized bed further comprises a connecting assembly connected between the first heat exchange tubes, 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 smaller than that of the connecting pieces used for connecting all the adjacent first heat exchange tubes.
2. The fluidized bed of claim 1, wherein: the fluidized bed further comprises a first circumferential acceleration mechanism located in the dilute phase zone stable fluidized section;
the first circumferential acceleration mechanism comprises a first annular pipe, a first air inlet pipe and a plurality of first air outlet pipes, wherein the axial lead of the first annular pipe extends along the up-down direction, the first air inlet pipe is communicated with the lower part of the first annular pipe, and the first air outlet pipes are communicated with the upper side part of the first annular pipe in a uniformly arranged mode at intervals;
the first air outlet pipe is obliquely 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 annular pipe are mutually angled.
3. The fluidized bed of claim 1, wherein: the fluidized bed further comprises a spraying mechanism positioned in the lower pipe box and a feeding pipe communicated with the feeding hole and penetrating through the spraying mechanism upwards;
the injection 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, a plurality of air outlet holes are formed in the top of the air inlet ring pipe, the angle between the injection 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 injection direction.
4. A fluidized bed according to claim 3, characterized in that: the fluidized bed further comprises a second circumferential acceleration mechanism located above the injection mechanism;
the second circumferential acceleration mechanism comprises a second annular pipe, a second air inlet pipe and a plurality of second air outlet pipes, wherein the axial lead of the second annular pipe extends along the up-down direction, the second air inlet pipe is communicated with the lower part of the second annular pipe, and the second air outlet pipes are communicated with the upper side part of the second annular pipe in a uniformly arranged mode at intervals;
the second air outlet pipe is obliquely 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 circular pipe are mutually angled.
5. The fluidized bed of claim 1, wherein: the fluidized bed further comprises a second heat exchange tube wound on the periphery of the outer side of the reaction cylinder.
6. The fluidized bed of claim 1, wherein: the reaction cartridge further includes a settling section connected above the dilute phase zone stable fluidization section.
7. The fluidized bed of claim 1, wherein: the fluidized bed further comprises a separation and recovery mechanism, wherein the separation and recovery mechanism comprises a main separator communicated with the discharge pipe and a main feed back pipe with one end communicated with the main separator, and the other end of the main feed back pipe is arranged in the reaction cylinder in a penetrating manner.
8. The fluidized bed of claim 7, wherein: the separation and recovery mechanism further comprises a secondary separator communicated with the primary separator, and a secondary feed back pipe with one end communicated with the secondary separator, wherein the other end of the secondary feed back pipe is arranged in the reaction cylinder in a penetrating manner.
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