CN205527778U - Hydrogenation fluidized bed reactor and have its polycrystalline silicon production system - Google Patents
Hydrogenation fluidized bed reactor and have its polycrystalline silicon production system Download PDFInfo
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- CN205527778U CN205527778U CN201620071808.3U CN201620071808U CN205527778U CN 205527778 U CN205527778 U CN 205527778U CN 201620071808 U CN201620071808 U CN 201620071808U CN 205527778 U CN205527778 U CN 205527778U
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Abstract
The utility model provides a hydrogenation fluidized bed reactor and have its polycrystalline silicon production system. Gas mixture that this hydrogenation fluidized reactor is connected including the order admit air section of thick bamboo section, reaction cylinder section and gas -solid cylinder section, wherein, the gas mixture admits air section of thick bamboo section and forms and mix an air cavity, and the gas mixture intracavity is provided with air inlet unit and gas distribution arrangement, and gas distribution arrangement and gas mixture admit air section of thick bamboo section to be connected, and gas distribution arrangement is near the reaction cylinder section, material feed opening has been seted up on the section of thick bamboo wall of reaction cylinder section, having seted up on the section of thick bamboo wall of gas -solid cylinder section and having generated the gas export, be provided with cyclone in the gas -solid cylinder section, cyclone's gas outlet and the export of formation gas are linked together. The utility model discloses a hydrogenation silicon tetrachloride process was complicated during prior art can be solved to the hydrogenation fluidized reactor, retrieved the big problem of the degree of difficulty.
Description
Technical field
This utility model relates to production of polysilicon and manufactures field, hydrogenates fluidized-bed reactor in particular to one and has it
Polycrystalline silicon production system.
Background technology
In polysilicon production process, reaction product has substantial amounts of silicon tetrachloride as by-product, polysilicon and four chlorinations
The yield ratio of silicon is about between 1:15～1:20, and the generation of Silicon chloride. has a strong impact on output efficiency and the production process of polysilicon
In energy-saving and cost-reducing needs.Further, the random discharge of Silicon chloride., easily pollute environment and threaten human health.
Processing mode to Silicon chloride. is to recycle it.The most both economical rationality, can effectively reduce again environmental pollution.
At present, the method recycled Silicon chloride. mainly has a following two:
One is as raw material to produce white carbon using Silicon chloride..Although the market demand capacity of current high-grade white carbon is relatively big,
But the production process of high-grade white carbon is harsh to the requirement of technique and equipment, therefore white carbon volume production relatively difficult to achieve；And it is low-grade
The market demand capacity of white carbon is limited.
Two is to use hydrogenation process that Silicon chloride. is carried out hydrogenation treatment.Under appropriate conditions, it is converted into after hydrogenation of silicon tetrachloride
Produce the raw material trichlorosilane of polysilicon.
To sum up consider, in polysilicon production process, it is generally preferable to Silicon chloride. is recycled by hydrogenization of silicon tetrachloride technique,
But hydrogenization of silicon tetrachloride complex technical process of the prior art, recovery difficult is big.
Utility model content
Main purpose of the present utility model is to provide a kind of polycrystalline silicon production system hydrogenating fluidized-bed reactor and having it, with
Solve hydrogenization of silicon tetrachloride complex technical process in prior art, the problem that recovery difficult is big.
To achieve these goals, according to an aspect of the present utility model, it is provided that a kind of hydrogenation fluidized reactor, including suitable
Gaseous mixture air induction mast section, reaction tube section and the gas-solid cylinder section that sequence connects, wherein, gaseous mixture air induction mast section forms mixed air cavity,
Distribution device in gas-fluid, gas it is provided with in being provided with the air intake installation for inputting mixed gas and mixed air cavity at mixed air cavity
Distribution apparatus is connected with gaseous mixture air induction mast section, and the position that distribution device in gas-fluid is between reaction tube section and air intake installation；
Material charging aperture is offered on the barrel of reaction tube section；Offering generation gas outlet on the barrel of gas solid separation cylinder section 30, gas-solid divides
Being provided with at least one cyclone separator away from cylinder section, the gas outlet of cyclone separator is connected with generating gas outlet.
Further, air intake installation includes: the first pipeline section, and the inlet end of the first pipeline section is installed along the bottom of gaseous mixture air induction mast section
Mouth extends outside；Second pipeline section, the second pipeline section and the first pipeline section are rotatably coupled, and the second pipeline section offers circumference and gives vent to anger
Mouthful.
Further, slag-drip opening is formed between the bottom installing port of the first pipeline section and gaseous mixture air induction mast section.
Further, the outlet side of the first pipeline section is provided with the interior clasp towards this pipeline section central axis, and the wall of interior clasp is opened
It is provided with the first limited impression；The air inlet of the second pipeline section is provided with the outer clasp coordinated with interior clasp hooking, and the pipe of the second pipeline section
The second limited impression is offered on wall；It is provided with locating part between first limited impression and the second limited impression.
Further, gaseous mixture air induction mast section is that flaring is arranged to the end being connected with reaction tube section by installing port end.
Further, air intake installation includes: air inlet pipeline section, and the first end of air inlet pipeline section extends the outside of gaseous mixture air induction mast section；
Annular gas transmission pipeline section, annular appendix section is positioned at the mixed air cavity of gaseous mixture air inlet pipeline section, annular gas transmission pipeline section and air inlet pipeline section
In connection, and annular gas transmission pipeline section, compartment of terrain offers multiple gas outlet.
Further, air intake installation includes: gaseous mixture annular duct, and gaseous mixture annular duct is positioned at gaseous mixture air induction mast section
Outside, multiple inlet pipe connections, multiple inlet pipe connections interval arrange, the first end of multiple inlet pipe connections with mix compression ring
Shape conveying pipe connection, the second end of multiple inlet pipe connections extends into the inside of gaseous mixture air induction mast section.
Further, distribution device in gas-fluid includes: gas distributing disc, and gas distributing disc is connected with the inwall of gaseous mixture air induction mast section,
Multiple tapped through hole is offered on gas distributing disc；Air outlet structure, air outlet structure includes inducing QI pipe fitting and inducing QI nut, airway
First end of part is spirally connected with tapped through hole, and inducing QI nut is screwed onto on inducing QI pipe fitting, the tube wall of the second end of inducing QI pipe fitting and inducing QI
Formed between the inwall of nut on air guide channel, and inducing QI nut and circumferentially offer gaseous mixture air guide port.
Further, gas distributing disc is spherical cap shape, and the spherical crown surface of gas distributing disc highlights towards air intake installation.
Further, the contour shape of the longitudinal section of gas distributing disc is trapezoidal, and gas distributing disc is prominent to air intake installation.
Further, the contour shape of the longitudinal section of gas distributing disc is triangle, and a drift angle of triangle fills towards air inlet
Put.
Further, gas distributing disc is writing board shape.
Further, the barrel of reaction tube section being further opened with conversion zone bleed outlet, conversion zone bleed outlet is positioned under reaction tube section
End.
Further, the barrel of reaction tube section is further opened with for temperature sensor mounted first installing hole and for installing
Second installing hole of pressure transducer.
Further, being provided with brokenly bubble aperture plate in reaction tube section, conversion zone bleed outlet is positioned at brokenly bubble aperture plate and gaseous mixture air induction mast section
Between.
Further, the barrel of gas solid separation cylinder section is further opened with the pressure releasing mouth for pressure of releasing.
Further, being also associated with tapering transition section between gas solid separation cylinder section and reaction tube section, tapering transition section is by gas solid separation
Cylinder section becomes tapered setting to reaction tube section.
According to another aspect of the present utility model, it is provided that a kind of polycrystalline silicon production system, polycrystalline silicon production system includes aforesaid
Hydrogenation fluidized reactor.
Application the technical solution of the utility model, applies four chlorinations to producing in polysilicon production process of this hydrogenation fluidized reactor
When silicon by-product reclaims, the mixed gas of Silicon chloride. with hydrogen is inputted by air intake installation, then by solid material from thing
Material charging aperture is sent into and fluidizes solid material, and the material after fluidisation and mixed gas carry out hydrogenation, thus generate three
Chlorine hydrogen silicon, then export after at least one cyclone separator carries out gas solid separation and reclaim trichlorosilane.This hydrogenation fluidized reaction
Device can carry out hydrogenation to the Silicon chloride. produced in polysilicon production process and reclaim, and completes tetrachloro in the flow process of same reactor
The hydrogenation process of SiClx, simplifies reaction process, reduces the hydrogenation recovery difficult of Silicon chloride..
Accompanying drawing explanation
The Figure of description of the part constituting the application is used for providing being further appreciated by of the present utility model, of the present utility model
Schematic description and description is used for explaining this utility model, is not intended that improper restriction of the present utility model.In the accompanying drawings:
Fig. 1 shows the structural representation of the first embodiment according to hydrogenation fluidized reactor of the present utility model；
Fig. 2 shows structure for amplifying schematic diagram at the A in Fig. 1；
Fig. 3 shows the structural representation of the distribution device in gas-fluid of Fig. 1；
Fig. 4 shows the structural representation of the air outlet structure in the distribution device in gas-fluid of Fig. 3；
Fig. 5 shows that the another kind of structure of the gas distributor in the first embodiment of hydrogenation fluidized reactor of the present utility model is shown
It is intended to；
Fig. 6 shows the structural representation of cyclone separator in Fig. 1；
Fig. 7 shows the structural representation of the second embodiment according to hydrogenation fluidized reactor of the present utility model；
Fig. 8 shows the structural representation of the air intake installation in Fig. 7；
Fig. 9 shows the structural representation of the 3rd embodiment according to hydrogenation fluidized reactor of the present utility model；
Figure 10 shows the structural representation of the air intake installation in Fig. 9.
Wherein, above-mentioned accompanying drawing includes the following drawings labelling:
10, gaseous mixture air induction mast section；11, air intake installation；
111, the first pipeline section；112, the second pipeline section；
12, distribution device in gas-fluid；121, gas distributing disc；
122, air outlet structure；1221, inducing QI pipe fitting；
1222, inducing QI nut；113, slag-drip opening；
114, air inlet pipeline section；115, annular gas transmission pipeline section；
116, gaseous mixture annular duct；117, inlet pipe connection；
20, reaction tube section；21, material charging aperture；
22, conversion zone bleed outlet；23, the first installing hole；
24, the second installing hole；30, gas solid separation cylinder section；
31, gas outlet is generated；32, cyclone separator；
321, separator changeover portion；322, separator cone section；
323, separator tangential inlet；324, separator valve；
33, pressure releasing mouth；40, locating part；
50, broken bubble aperture plate；60, tapering transition section.
Detailed description of the invention
It should be noted that in the case of not conflicting, the embodiment in the application and the feature in embodiment can be mutually combined.
Describe this utility model below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
Solid material in embodiment of the present utility model is preferably material silica flour.
As it is shown in figure 1, first embodiment of the present utility model provides a kind of hydrogenation fluidized reactor, this reactor inside diameter scope
Being 1000mm to 4500mm, its ratio of height to diameter is 6:1 to 9:1, and this hydrogenation fluidized reactor includes that the gaseous mixture being linked in sequence enters
Inflator section 10, reaction tube section 20 and gas-solid cylinder section 30, the hydrogenation section carrying out hydrogenation in reaction tube section 20
Highly being about 2000mm to 15000mm, wherein, gaseous mixture air induction mast section 10 forms mixed air cavity, is provided with at mixed air cavity
In the air intake installation 11 inputting gaseous mixture and mixed air cavity, be provided with distribution device in gas-fluid 12, distribution device in gas-fluid 12 with
Gaseous mixture air induction mast section 10 connects, and the position that distribution device in gas-fluid 12 is between reaction tube section 20 and air intake installation 11,
Offer material charging aperture 21 on the barrel of reaction tube section 20, the barrel of gas solid separation cylinder section 30 offer generation gas outlet 31,
Being provided with at least one cyclone separator 32 at gas solid separation cylinder section 30, in the present embodiment, cyclone separator 32 can be arranged
1,2,3 or 2n (n >=2) are individual, and the gas outlet of cyclone separator 32 is connected, preferably with generating gas outlet 31
Ground, generates gas outlet and is opened in the bottom of gas solid separation cylinder section 30.
When applying this hydrogenation fluidized reactor that the silicon tetrachloride byproduct produced in polysilicon production process is reclaimed, by tetrachloro
SiClx is inputted by air intake installation 11 with the mixed gas of hydrogen, is then sent into and to solid material from material charging aperture by solid material
Fluidizing, the material after fluidisation and mixed gas carry out hydrogenation, thus generate trichlorosilane, then through at least one whirlwind
Separator 32 exports after carrying out gas solid separation and reclaims trichlorosilane.This hydrogenation fluidized reactor can be to polysilicon production process
The Silicon chloride. of middle generation carries out hydrogenation and reclaims, and completes the hydrogenation process of Silicon chloride. in the flow process of same reactor, simplifies anti-
Answer flow process, reduce the hydrogenation recovery difficult of Silicon chloride..
Cyclone separator 32 can be built in the inside of gas solid separation cylinder section 30, or the operative body of cyclone separator 32 is external
Outside in gas solid separation cylinder section 30.In the first embodiment, preferably cyclone separator 32 is built in gas solid separation cylinder section
The inside of 30.
As in figure 2 it is shown, the air intake installation 11 of the hydrogenation fluidized reactor of first embodiment includes the first pipeline section 111 and the second pipeline section
112, the inlet end of the first pipeline section 111 extends to outside along the bottom installing port of gaseous mixture air induction mast section 10, thus will be many in production
After the by-product gas containing gas phase Silicon chloride. produced in crystal silicon technical process mixes with hydrogen, by the air inlet of the first pipeline section 111
End input.In the first embodiment, slag-drip opening is formed between the bottom installing port of the first pipeline section 111 and gaseous mixture air induction mast section 10
113.Second pipeline section 112 is rotatably coupled with the first pipeline section 111, and the second pipeline section 112 offers circumference gas outlet.When solid
Body material inputs from material charging aperture 21, and enters with the Silicon chloride. from the mixed gas of circumference gas outlet output after fluidisation
Row hydrogenation, thus generate trichlorosilane to realize the silicon tetrachloride as by-product in polysilicon production process is reclaimed.?
Solid material is carried out in fluid mapper process, there is a little solid material and do not fluidize completely or hydriding process generates other
The solid slag that cannot dissolve, the bottom of these solid deposits to gaseous mixture air induction mast section 10, then will from slag-drip opening 113
These solid slags emit.
Specifically, the outlet side of the first pipeline section 111 is provided with the interior clasp towards this pipeline section central axis, and the wall of interior clasp is opened
Being provided with the first limited impression, the air inlet of the second pipeline section 112 is provided with the outer clasp coordinated with interior clasp hooking, and the second pipeline section
Offer the second limited impression on the tube wall of 112, between the first limited impression and the second limited impression, be provided with locating part 40.Interior button
Carry out after assembling completes by locating part 40 between hook and outer clasp, can be real between the first pipeline section 111 and the second pipeline section 112
Connect the most in relative rotation, and, the inner surface away from the end of the first pipeline section 111 of the second pipeline section 112 is set to smooth surface,
Or the inner surface of this end be set to according to certain rules with the matsurface of direction cutting.During gaseous mixture inputs, due to
Gaseous mixture has flow velocity and pressure, thus the inner surface that mixed airflow is to the end away from the first pipeline section 111 of the second pipeline section 112 is also
The second pipeline section 112 can be made to rotate relative to the first pipeline section 111, and then gaseous mixture is from the output of circumference gas outlet.The second pipe rotated
The gaseous mixture that section 112 can regulate in mixed air cavity is evenly distributed, and, the second pipeline section 112 of rotation can be in mixed air cavity
Gaseous mixture be stirred, the distribution of the gaseous mixture of further homogeneous mixture intracavity.
Locating part 40 can be with spacing steel ring, it is also possible to be multiple spacing steel balls.First pipeline section 111 and the second pipeline section 112 by with
Occlusion between locating part 40, it is possible to stably limit the relative position between the first pipeline section 111 with the second pipeline section 112 so that the
Both when two pipeline sections 112 rotate relative to the first pipeline section 111 without departing from.
In the present first embodiment, gaseous mixture air induction mast section 10 is flaring by installing port end to the end being connected with reaction tube section 20
Arrange.The slag charge fallen can be gathered collection by the gaseous mixture air induction mast section 10 so arranged so that slag charge can be intensively
Discharge from slag-drip opening 113.
Shown in as shown in Figure 1, Figure 3 and Figure 4, the distribution device in gas-fluid 12 of first embodiment includes gas distributing disc 121 and goes out depressed
Structure 122, gas distributing disc 121 is connected with the inwall of gaseous mixture air induction mast section 10, and gas distributing disc 121 offers multiple spiral shell
Stricture of vagina through hole, air outlet structure 122 includes inducing QI pipe fitting 1221 and inducing QI nut 1222, the first end of inducing QI pipe fitting 1221 and screw thread
Through hole is spirally connected, and inducing QI nut 1222 is screwed onto on inducing QI pipe fitting 1221, the tube wall of the second end of inducing QI pipe fitting 1221 and inducing QI spiral shell
Formed between the inwall of female 1222 on air guide channel, and inducing QI nut 1222 and circumferentially offer gaseous mixture air guide port.Multiple screw threads
Between through hole, arrangement forms the geometries such as equilateral triangle, square or circular concentric, and the spacing distance between Kong Yukong is
50mm to 250mm.Enter the gaseous mixture of distribution device in gas-fluid 12, first pass through in the central aeration road on inducing QI pipe fitting 1221,
Then this central aeration road enters air guide channel, by gaseous mixture air guide port input reaction tube section 20.Distribution device in gas-fluid 12
Ensure that gaseous mixture is evenly distributed on reaction tube section 20 cross section.
The most in the present first embodiment, gas distributing disc 121 is spherical cap shape, and the spherical crown surface court of gas distributing disc 121
Prominent to air intake installation 11.Certainly, also can be selected for flat gas distributing disc.Comparatively speaking, the ball of this first embodiment
The gas distributing disc 121 of crown shape is better than flat gas distributing disc according to the distribution of the gaseous mixture rate of climb, and therefore, this is the years old
The gas distributing disc 121 of the one preferred spherical cap shape of embodiment.Additionally, as it is shown in figure 5, the gas distributing disc 121 of first embodiment
The contour shape of longitudinal section be trapezoidal, and gas distributing disc 121 is prominent to air intake installation 11.Or, gas distributing disc 121
For writing board shape, and the gas distributing disc 121 of writing board shape is across in mixed air cavity.Or, the gas of first embodiment
The contour shape of the longitudinal section of distributing disc 121 is triangle, and a drift angle of triangle is towards air intake installation 11, when selecting three
During dihedral gas distributing disc 121, at the drift angle of air intake installation 11, offer opening, and connecting pipeline is installed on opening, should
Connecting pipeline is extended outside by the bottom installing port of gaseous mixture air induction mast section 10, and now this connecting pipeline and the first pipeline section 111 are also
Row ground is stretched out by installing port, and so, the slag charge of precipitation above gas distributing disc 121 can be exported by this connecting pipeline, and,
Also slag-drip opening 113 is formed between connecting pipeline and installing port.
Distribution device in gas-fluid 12 in this first embodiment ensure that the optimal gaseous mixture needed for obtaining greater efficiency hydrogenation enters
Airflow field state.
As it is shown in figure 1, in the present first embodiment, the barrel of reaction tube section 20 is further opened with conversion zone bleed outlet 22, reaction
Section bleed outlet 22 is positioned at the lower end of described reaction tube section 20.When the liquid in reaction tube section 20 is too much, this reaction can be passed through
Section bleed outlet 22 is released, to reduce the pressure store in reaction tube section 20.
Specifically, the barrel of the reaction tube section 20 of this first embodiment is further opened with installing for temperature sensor mounted first
Hole 23 and for installing the second installing hole 24 of pressure transducer.During reaction, passed by temperature sensor and pressure
Sensor monitors the temperature in hydrogenation fluidized reactor and pressure in real time, when the temperature hydrogenated in fluidized reactor, hypertonia,
Need inside reactor is carried out pressure release, in the present first embodiment, the barrel of gas solid separation cylinder section 30 is further opened with for letting out
Bleed off pressure the pressure releasing mouth 33 of power.Preferably, this pressure releasing mouth 33 is opened at the tip position of gas solid separation cylinder section 30 and (is somebody's turn to do
Hydrogenation fluidized reactor is placed longitudinally, and gaseous mixture air induction mast section 10 is positioned at bottom, and gas solid separation cylinder section 30 is positioned at and goes up most
End, reaction tube section 20 is centrally located).The temperature and pressure detected by temperature sensor and pressure transducer,
When hydrogenating the hypertonia in fluidized reactor, carry out pressure discharge operations by this pressure releasing mouth 33, to ensure hydrogenation fluidized reaction
Pressure within device is maintained in normally-pressured neighbor.
Solid material puts into after reaction tube section 20, solid material be fluidized and with mixed gas generation hydrogenation, in solid material
During being fluidized and hydrogenation occurring, in hydrogenation fluidized reactor, produce bubble, in preventing aeration reactor
Hydrogenation, and avoid the output of aeration product or slag charge, therefore, bubble grid be installed brokenly in reaction tube section 20
Net 50, conversion zone bleed outlet 22 is between broken bubble aperture plate 50 and gaseous mixture air induction mast section 10.
After hydrogenation generates trichlorosilane, the mixing after hydrogenation generates gas and rises, in order to it is raw to promote mixing
Become gas to enter the pressure of cyclone separator 32, therefore, between gas solid separation cylinder section 30 and reaction tube section 20, be also associated with taper
The section of crossing 60, tapering transition section 60 by gas solid separation cylinder section 30 to reaction tube section 20 in tapered setting.Cylinder tapering transition section 60 makes
The rate of climb of mixing generation gas reduces, and mixes the pressure rising generating gas, thus mixes and generate gas with bigger pressure entrance
Cyclone separator 32 carries out lock out operation.
As shown in figures 1 to 6, cyclone separator 32 separate during, mixing generate gas along cyclone separator 32 point
Cyclone separator 32 is entered internal from device tangential inlet 323, the screw that gas-solid mixture seat is downward, sequentially pass through separator
Cone section 322 and separator changeover portion 321, it is achieved after gas solid separation, mixing generation gas goes out along the gas of cyclone separator 32
Mouth is to generating gas outlet 31 conveying, thus exports generation gas.Solid material deposits to rotation along the internal face of cyclone separator 32
In the long straight length of wind separator 32 bottom.When the cumulative weight of solid material exceedes the weight that separator valve 324 is born
Time, separator valve opens under the promotion of solid material gravity that (certainly, separator valve 324 can also use dynamic Control
The valve being turned on and off), solid material falls back to the mixed gas continued in reaction tube section 20 with Silicon chloride. and hydrogen to be carried out
(aperture position of this separator valve 324 is arranged on the top of upper end of reaction tube section 20 to hydrogenation, and slightly higher with reaction
Cylinder section 20 is advisable, at the height higher than the 200mm to 1500mm above reaction tube section 20).When solid material is from dividing
After device valve 324 exports, separator valve is closed, until after solid material cumulative weight, being again turned on, so follows
Ring.Cyclone separator 32 can preferably isolate solid and gas in the gas-solid mixture after reaction, after gas solid separation,
Solid recovery utilization rate is up to 99.9%.The setting of cyclone separator 32, substantially increases the utilization rate of solid material, simplifies
Subsequent technique processes requirement, reduces the difficulty that gas-solid mixture carries out during subsequent technique separating-purifying.
As it is shown in fig. 7, it illustrates the structural representation of the second embodiment of hydrogenation fluidized reactor of the present utility model.Second
Embodiment has following difference compared with first embodiment.Air intake installation 11 includes air inlet pipeline section 114 and annular appendix
Section 115.As shown in Figure 8, the first end of air inlet pipeline section 114 extends the outside of gaseous mixture air induction mast section 10, annular appendix
Section 115 is positioned at the mixed air cavity of gaseous mixture air induction mast section 10, and annular gas transmission pipeline section 115 connects with air inlet pipeline section 114, and
On annular gas transmission pipeline section 115, compartment of terrain offers multiple gas outlet.In order to make gaseous mixture going out from annular gas transmission pipeline section 115
QI KOU output is evenly distributed in being received in mixed air cavity, and therefore, multiple gas outlets annularly gas transmission pipeline section 115 is circumferentially distributed, and
It is respectively mounted jet nozzle on each gas outlet, utilizes jet nozzle that gaseous mixture uniformly sprays to mixed air cavity.As it is shown in fig. 7,
The hydrogenation fluidized reactor of the second embodiment is preferably by the distribution device in gas-fluid 12 of the gas distributing disc 121 of triangle.Second
Embodiment is compared with first embodiment, and in addition to above-mentioned difference, remaining structure is the most identical, thus does not repeats them here.
As shown in Figure 9 and Figure 10, it illustrates the structural representation of the hydrogenation fluidized reactor of the 3rd embodiment of the present utility model.
Compared with first embodiment, the 3rd embodiment has following difference.In the third embodiment, air intake installation includes mixing
Gas ring shape conveying pipe 116 and multiple inlet pipe connection 117, wherein, gaseous mixture annular duct 116 is positioned at gaseous mixture air induction mast section
The outside of 10, multiple inlet pipe connections 117 interval is arranged, and multiple inlet pipe connection 117 is circumferentially, multiple air inlets
First end of connecting tube 117 connects with gaseous mixture annular duct 116, and the second of multiple inlet pipe connections 117 extends into gaseous mixture
In the mixed air cavity of air induction mast section 10.In the third embodiment, gas distributing disc 121 uses the distribution device in gas-fluid of spherical cap shape
12.Further, the bottom installing port of the gaseous mixture air induction mast section 10 in the 3rd embodiment defines slag-drip opening 113.3rd embodiment
Compared with first embodiment, in addition to above-mentioned difference, remaining structure is the most identical, thus does not repeats them here.
According to another aspect of the present utility model, it is provided that a kind of polycrystalline silicon production system, this polycrystalline silicon production system includes aforementioned
Hydrogenation fluidized reactor.
The foregoing is only preferred embodiment of the present utility model, be not limited to this utility model, for this area
For technical staff, this utility model can have various modifications and variations.All within spirit of the present utility model and principle, institute
Any modification, equivalent substitution and improvement etc. made, within should be included in protection domain of the present utility model.
Claims (18)
1. a hydrogenation fluidized reactor, it is characterised in that include gaseous mixture air induction mast section (10), the reaction tube section (20) being linked in sequence
With gas-solid cylinder section (30), wherein,
Described gaseous mixture air induction mast section (10) forms mixed air cavity, is provided with for inputting gaseous mixture at described mixed air cavity
Air intake installation (11) and described mixed air cavity in be provided with distribution device in gas-fluid (12), described distribution device in gas-fluid
(12) it is connected with described gaseous mixture air induction mast section (10), and described distribution device in gas-fluid (12) is positioned at described reaction tube
Position between section (20) and described air intake installation (11)；
Material charging aperture (21) is offered on the barrel of described reaction tube section (20)；
Generation gas outlet (31), described gas solid separation cylinder section (30) is offered on the barrel of described gas solid separation cylinder section (30)
Place is provided with at least one cyclone separator (32), the gas outlet of described cyclone separator (32) and described generation gas
Outlet (31) is connected.
Hydrogenation fluidized reactor the most according to claim 1, it is characterised in that described air intake installation (11) including:
First pipeline section (111), the inlet end of described first pipeline section (111) is along the end of described gaseous mixture air induction mast section (10)
Portion's installing port extends outside；
Second pipeline section (112), described second pipeline section (112) is rotatably coupled with described first pipeline section (111), institute
State and on the second pipeline section (112), offer circumference gas outlet.
Hydrogenation fluidized reactor the most according to claim 2, it is characterised in that described first pipeline section (111) mixes with described
Slag-drip opening (113) is formed between the bottom installing port of gas air induction mast section (10).
Hydrogenation fluidized reactor the most according to claim 2, it is characterised in that
The outlet side of described first pipeline section (111) is provided with the interior clasp towards this pipeline section central axis, described interior clasp
The first limited impression is offered on wall；
The air inlet of described second pipeline section (112) is provided with the outer clasp coordinated with described interior clasp hooking, and described second
The second limited impression is offered on the tube wall of pipeline section (112)；
Locating part (40) it is provided with between described first limited impression and described second limited impression.
Hydrogenation fluidized reactor the most according to claim 2, it is characterised in that described gaseous mixture air induction mast section (10) is by institute
Stating installing port end is that flaring is arranged to the end being connected with described reaction tube section (20).
Hydrogenation fluidized reactor the most according to claim 1, it is characterised in that described air intake installation (11) including:
Air inlet pipeline section (114), the first end of described air inlet pipeline section (114) extends described gaseous mixture air induction mast section (10)
Outside；
Annular gas transmission pipeline section (115), described annular gas transmission pipeline section (115) is positioned at described gaseous mixture air induction mast section (10)
Mixed air cavity in, described annular gas transmission pipeline section (115) connects with described air inlet pipeline section (114), and described annular is defeated
The upper compartment of terrain of trachea section (115) offers multiple gas outlet.
Hydrogenation fluidized reactor the most according to claim 1, it is characterised in that described air intake installation (11) including:
Gaseous mixture annular duct (116), described gaseous mixture annular duct (116) is positioned at described gaseous mixture air induction mast
The outside of section (10)；
Multiple inlet pipe connections (117), multiple described inlet pipe connections (117) interval is arranged, and multiple described air inlets are even
First end of adapter (117) connects with described gaseous mixture annular duct (116), multiple described inlet pipe connections (117)
The second end extend in the mixed air cavity of described gaseous mixture air induction mast section (10).
Hydrogenation fluidized reactor the most according to claim 1, it is characterised in that distribution device in gas-fluid (12) including:
The inwall of gas distributing disc (121), described gas distributing disc (121) and described gaseous mixture air induction mast section (10)
Connect, described gas distributing disc (121) offers multiple tapped through hole；
Air outlet structure (122), described air outlet structure (122) includes inducing QI pipe fitting (1221) and inducing QI nut (1222),
First end of described inducing QI pipe fitting (1221) is spirally connected with described tapped through hole, and described inducing QI nut (1222) is screwed onto institute
State on inducing QI pipe fitting (1221), the tube wall of the second end of described inducing QI pipe fitting (1221) and described inducing QI nut (1222)
Inwall between formed on air guide channel, and described inducing QI nut (1222) and circumferentially offer gaseous mixture air guide port.
Hydrogenation fluidized reactor the most according to claim 8, it is characterised in that described gas distributing disc (121) is spherical
Shape, and the spherical crown surface of described gas distributing disc (121) is prominent towards described air intake installation (11).
Hydrogenation fluidized reactor the most according to claim 8, it is characterised in that the longitudinal section of described gas distributing disc (121)
Contour shape be trapezoidal, and described gas distributing disc (121) is prominent to described air intake installation (11).
11. hydrogenation fluidized reactors according to claim 8, it is characterised in that the longitudinal section of described gas distributing disc (121)
Contour shape be triangle, and a drift angle of described triangle is towards described air intake installation (11).
12. hydrogenation fluidized reactors according to claim 8, it is characterised in that described gas distributing disc (121) is plate shaped
Shape.
13. hydrogenation fluidized reactors according to claim 1, it is characterised in that on the barrel of described reaction tube section (20) also
Offering conversion zone bleed outlet (22), described conversion zone bleed outlet (22) is positioned at the lower end of described reaction tube section (20).
14. hydrogenation fluidized reactors according to claim 13, it is characterised in that on the barrel of described reaction tube section (20) also
Offer for temperature sensor mounted first installing hole (23) and for installing the second installing hole of pressure transducer
(24)。
15. hydrogenation fluidized reactors according to claim 13, it is characterised in that be provided with brokenly in described reaction tube section (20)
Bubble aperture plate (50), described conversion zone bleed outlet (22) is positioned at described broken bubble aperture plate (50) and described gaseous mixture air induction mast section
(10) between.
16. hydrogenation fluidized reactors according to claim 1, it is characterised in that on the barrel of gas solid separation cylinder section (30) also
Offer the pressure releasing mouth (33) for pressure of releasing.
17. hydrogenation fluidized reactors according to claim 16, it is characterised in that described gas solid separation cylinder section (30) is with described
Being also associated with tapering transition section (60) between reaction tube section (20), described tapering transition section (60) is by described gas solid separation
Cylinder section (30) becomes tapered setting to described reaction tube section (20).
18. 1 kinds of polycrystalline silicon production systems, it is characterised in that described polycrystalline silicon production system includes any one of claim 1 to 17
Described hydrogenation fluidized reactor.
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| CN201620071808.3U CN205527778U (en) | 2016-01-25 | 2016-01-25 | Hydrogenation fluidized bed reactor and have its polycrystalline silicon production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502411A (en) * | 2016-01-25 | 2016-04-20 | 中国恩菲工程技术有限公司 | Hydrogenated fluidized bed reactor and polycrystalline silicon production system with same |
| US10118144B2 (en) | 2017-03-31 | 2018-11-06 | Uop Llc | Vessel for removing hydrocarbons on catalyst |
-
2016
- 2016-01-25 CN CN201620071808.3U patent/CN205527778U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502411A (en) * | 2016-01-25 | 2016-04-20 | 中国恩菲工程技术有限公司 | Hydrogenated fluidized bed reactor and polycrystalline silicon production system with same |
| US10118144B2 (en) | 2017-03-31 | 2018-11-06 | Uop Llc | Vessel for removing hydrocarbons on catalyst |
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