CN201605166U - Hydrogenation silicon tetrachloride boiling bed reactor - Google Patents
Hydrogenation silicon tetrachloride boiling bed reactor Download PDFInfo
- Publication number
- CN201605166U CN201605166U CN2009202739629U CN200920273962U CN201605166U CN 201605166 U CN201605166 U CN 201605166U CN 2009202739629 U CN2009202739629 U CN 2009202739629U CN 200920273962 U CN200920273962 U CN 200920273962U CN 201605166 U CN201605166 U CN 201605166U
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- silicon tetrachloride
- separator
- bed reactor
- gas distribution
- hydrogenization
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Abstract
The utility model relates to a hydrogenation silicon tetrachloride boiling bed reactor, which comprises a primary gas distributing tray and a secondary gas distributing tray. The secondary gas distributing tray includes a distributing plate; axial vent holes are distributed on the distributing plate; the lower ends of the axial vent holes are communicated with the lower portion of the distributing plate; the upper ends of the axial vent holes are closed; pluralities of radial vent holes are arranged on the lateral walls or the tops of the axial vent holes; and the radial vent holes are communicated with the upper end of the distributing plate. Besides, a separator is further arranged at the position of an outlet of the hydrogenation silicon tetrachloride boiling bed reactor; an inlet of the separator is in a tangential direction; a tapered section arranged at the lower end of the separator can lead hydrogen to spirally move from top to bottom; and a gravity opening valve arranged at the bottom end of the separator decreases the carrying rate of hydrogenation gas silica powders, reduces material loss and improves material using ratio to a large extent. The hydrogenation silicon tetrachloride boiling bed reactor is reasonable in structure and simple and convenient in operation, and greatly improves reaction efficiency and the material using ratio.
Description
Technical field
The utility model relates to a kind of reactor of hydrogenization of silicon tetrachloride, particularly a kind of hydrogenization of silicon tetrachloride ebullated bed reactor that has gas distribution dish and separator belongs to photovoltaic industrial technology field.
Background technology
Polysilicon is the important raw and processed materials of semi-conductor, large-scale integrated circuit and solar energy industry, pulling and golden eggs in the photovoltaic industrial market are induced down, and various places polysilicon project starts one after another, and the polysilicon industrial prospect is wide, development is swift and violent, has become the focus of investment in China.
Simultaneously, production of polysilicon pollutes easily, produces 1000 tons of polysilicons and will generate about 15000 tons of SiCl4 (being silicon tetrachloride), SiCl4 has moderate toxicity, easily deliquescence becomes silicic acid and hydrogenchloride, is not good at just can causing very big pollution to environment if handle, and human body is also had very big harm.How processing of SiC l4 becomes one of focal issue of polysilicon industry.Present stage, part enterprise produces white carbon black with SiCl4, and its economic benefit is far below polysilicon, and market dialogue sooty demand also supply exceed demand; Other has part polysilicon enterprise to adopt hot hydride process processing of SiC l4, but has shortcomings such as transformation efficiency is low, energy consumption is high, facility investment is big.The method investment of above-mentioned processing of SiC l4 is high, income is low, has increased very high cost pressure to enterprise, causes indivedual illegal enterprises disorderly disorderly to arrange SiCl4, has caused the serious environmental pollution.
The utility model content
In order effectively to handle the silicon tetrachloride in the polysilicon production process, the utility model provides a kind of hydrogenization of silicon tetrachloride ebullated bed reactor, this ebullated bed reactor is hydrogenization of silicon tetrachloride effectively, generate the starting material SiHCl3 of polysilicon, have transformation efficiency height, low power consumption and other advantages, make polysilicon production process form an endless chain simultaneously, improved economic benefit effectively, reduced environmental pollution.
To achieve these goals, hydrogenization of silicon tetrachloride ebullated bed reactor of the present utility model, include the conversion zone, expanding reach and the segregation section that link successively from bottom to top, also be equiped with the outlet of material inlet and hydrogenation gas in the top of described reactor, described segregation section is equiped with the separator that links with described hydrogenation gas outlet bottom; Bottom in described reactor also is equiped with the maintenance end socket, is equiped with combi inlet port and slag-drip opening on this maintenance end socket; Between described maintenance end socket and conversion zone, be equiped with gas distribution dish and secondary air distributing disc from bottom to top successively.
As a kind of preferred version, a described gas distribution dish is connected with described combi inlet port, and this gas distribution dish also is connected with the peripheral tube that is installed in a described gas distribution dish outside by airway.
As a kind of preferred version, described peripheral tube ringwise, rich font or Polygons.
As a kind of preferred version, evenly be laid with through hole in the bottom of described peripheral tube.
As a kind of preferred version, described secondary air distributing disc includes gas distribution grid, the pipe cap that is equiped with the axial thread through hole and links with described tapped through hole on described gas distribution grid.
As a kind of preferred version, described pipe cap is convexly set in described gas distribution grid, the periphery at itself and the described gas distribution grid place of linking be provided with the threaded portion in order to the tapped through hole of described gas distribution grid with thread connection.
As a kind of preferred version, be provided with axial ventilating pit in the described pipe cap, the lower end of this axial ventilating pit is connected with the bottom of described gas distribution grid, the upper end closed of this axial ventilating pit.
As a kind of preferred version, described pipe cap also is equiped with radially ventilating pit, and it evenly is laid in the sidewall of described axial ventilating pit or end and is connected with the top of described gas distribution grid.
As a kind of preferred version, the upper end of described separator is provided with the separator tangential inlet in tangential direction, and the bottom of described separator is equiped with tapered separator awl section, is equiped with the gravity open valve in the bottom of this separator awl section.
The utility model comprises following three designs:
First design: a kind of ebullated bed reactor of hydrogenization of silicon tetrachloride is provided, and this designs the hydrogenation ability of main augmenting response device.
Second design: the secondary air distributing disc that provides a kind of hydrogenization of silicon tetrachloride ebullated bed reactor to use, the main fluidization quality that improves ebullated bed reactor of this design;
The 3rd design: the separator that provides a kind of hydrogenization of silicon tetrachloride ebullated bed reactor to use, the main silica flour carrying rate that reduces gas outlet hydrogenation gas of this design.
In order to realize first design, the utility model is taked following scheme:
A kind of ebullated bed reactor that is used for hydrogenization of silicon tetrachloride, this ebullated bed reactor comprises the conversion zone and the upper extension section of bottom, the conversion zone bottom is provided with the maintenance end socket, the maintenance end socket is provided with combi inlet port and slag-drip opening, expanding reach top is provided with the outlet of hydrogenation gas, material inlet, be provided with the gas distribution dish between conversion zone bottom and the maintenance end socket, this gas distribution dish adopts second described distributing disc of design.
Further, the gas mixture ingress also is provided with distributing disc one time.One time distributing disc is different from second distributing disc described in the design, and this distributing disc helps gas mixture evenly to enter conversion zone.Further, one time distributing disc is provided with peripheral tube, and peripheral tube can be ringwise, rich font or Polygons, and the peripheral tube bottom has several through holes.
Hydrogenation gas outlet lower end is provided with separator, and this separator adopts following the third to design described separator, helps reducing the silica flour carrying rate of hydrogenation gas.Further, separator is provided with tangential inlet, and the lower end is provided with the gravity open valve, and this valve utilizes gravity principle to open and close automatically.
In order to realize second design, the utility model is taked following scheme:
A kind of secondary air distributing disc that is used for the hydrogenization of silicon tetrachloride ebullated bed reactor, described secondary air distributing disc comprises grid distributor, uniform several tapped through holes on the grid distributor, be provided with pipe cap in the tapped through hole, pipe cap has outside screw, and its inside is provided with axial ventilating pit, axially the ventilating pit lower end is communicated with the grid distributor bottom, the axial upper end closed of ventilating pit, axially ventilating pit along sidewall or end uniform several ventilating pits radially, radially the ventilating pit upper end is connected with the top of grid distributor.
Further, above-mentioned pipe cap is made up of cap shell and threaded portion, and the cap shell is to protrude the pattern setting of gas distribution dish, and the threaded portion is connected with tapped through hole by screw thread.Further, radially ventilating pit is a plurality of, can be arranged on the cap shell side wall, also can be arranged on cap shell end.
In order to realize the 3rd design, the utility model adopts following scheme:
A kind of separator that is used for the hydrogenization of silicon tetrachloride ebullated bed reactor, this separator is provided with tangential inlet, and this inlet guiding gas mixture enters separator along the direction of tangent line, and separator lower end is the awl section, and the bottom is provided with the gravity open valve.
By above-mentioned design, transformation efficiency height, the fluidization quality of hydrogenization of silicon tetrachloride ebullated bed reactor of the present utility model is good, throughput is big, single device year treatment capacity can reach 30000～50000 tons.
Description of drawings
Fig. 1 is the structural representation of the utility model hydrogenization of silicon tetrachloride ebullated bed reactor;
Fig. 2 is the structural representation of secondary air distributing disc of the present utility model;
Fig. 3 is a cyclone separator arrangement synoptic diagram of the present utility model;
Fig. 4 a, Fig. 4 b and Fig. 4 c are the structural representations of pipe cap of the present utility model;
Fig. 5 is the structural representation of a gas distribution dish of the present utility model.
Wherein, the 1st, conversion zone, the 2nd, expanding reach, the 3rd, separator, the 4th, the outlet of hydrogenation gas, the 5th, material inlet, the 6th, the secondary air distributing disc, 7 is gas distribution dishes, the 8th, maintenance end socket, the 9th, combi inlet port, the 10th, gas distribution grid, 11 tapped through holes, the 12nd, pipe cap, the 13rd, axial ventilating pit, the 14th, ventilating pit radially, 15 threaded portions, the 16th, separator tangential inlet, the 17th, separator awl section, the 18th, gravity open valve, the 19th, slag-drip opening, the 20th, airway, the 21st, peripheral tube, the 22nd, the through hole of peripheral tube.
Embodiment
Below in conjunction with accompanying drawing concrete structure of the present utility model is further described, but the utility model is not limited to described embodiment.
As shown in Figure 1, the hydrogenization of silicon tetrachloride ebullated bed reactor from bottom to top comprises conversion zone 1 and expanding reach 2, also be equiped with material inlet 5 and hydrogenation gas outlet 4 in the top of described reactor, hydrogenation gas exports 4 places and is provided with separator 3, be equiped with maintenance end socket 8 in the bottom of described reactor, between described maintenance end socket 8 and conversion zone 1, be equiped with gas distribution dish 7 and secondary air distributing disc 6.Maintenance end socket 8 is provided with combi inlet port 9 and slag-drip opening 19, and hydrogenation gas outlet 4 is arranged at expanding reach 2 tops, and hydrogenation gas is by separating through separator 3 before the hydrogenation gas outlet 4.
Please be simultaneously in conjunction with Fig. 1 and Fig. 3, separator 3 upper ends are provided with separator tangential inlet 16, separator 3 lower ends are provided with gravity open valve 18, go into the material of separator 3 and after running up to certainweight, fall back to once more in the conversion zone 1 and react to guarantee to be hydrogenated the band of gas, to reduce the silica flour carrying rate of hydrogenation gas.
Please be simultaneously in conjunction with Fig. 1 and Fig. 5, one time gas distribution dish 7 is conducted with combi inlet port 9 one ends, by intermediary airway 20 gas mixture is imported peripheral tube 21, and peripheral tube 21 can be rendered as annular, rich font or Polygons, its uniform several through holes 22 in bottom.
Please be simultaneously in conjunction with Fig. 1 and Fig. 2, secondary air distributing disc 6 comprises grid distributor 10, uniform distribution is provided with several tapped through holes 11 on the grid distributor 10, is provided with pipe cap 12 in the tapped through hole 11.
Please be simultaneously in conjunction with Fig. 1, Fig. 2 and Fig. 4 a to Fig. 4 c, the pipe cap 12 outer threaded portions 15 that are provided with, pipe cap 12 and grid distributor 10 are by being threaded, pipe cap 12 protrudes grid distributor 10 and is provided with, be provided with axial ventilating pit 13 in the pipe cap 12, axially ventilating pit 13 lower ends are communicated with the bottom of grid distributor 10, the upper end closed of the axial ventilating pit 13 of pipe cap.Axially ventilating pit 13 along sidewall or end uniform several ventilating pits 14 radially, radially ventilating pit 14 evenly is arranged on the pipe cap 12 and with grid distributor 10 tops and is communicated with.
Material enters ebullated bed reactor by material inlet 5, because the action of gravity meeting drops down onto secondary air distributing disc 6 tops of conversion zone 1.Gas mixture enters distributing disc 7 one time by gas feed 9, by entering conversion zone under the gas port of a distributing disc 7 uniformly and stably, further gas mixture is by the pipe cap 12 of setting in the secondary air distributing disc 6, under the water conservancy diversion of the axial ventilating pit 13 of pipe cap 12 and ventilating pit 14 radially, gas mixture uniform stabilization once more is blown into conversion zone 1 with the material on the secondary air distributing disc 6 and reacts.The hydrogenation gas that generates carries the part silicon powder particle, enter separator 3 through the tangential inlet 16 from separator behind the expanding reach 2, hydrogenation gas rotatablely moves as spiral in separator 3, eddy flow is to separator awl section 17 bottoms, rise along the axis direction rotation again, the silicon powder particle that carries in the hydrogenation gas is thrown to the wall of separator 3 under action of centrifugal force, deposit to the separator bottom along wall, through after the separation of separator 3, hydrogenation gas is discharged from hydrogenation gas outlet 4, separator 3 lower ends are provided with gravity open valve 18, when silicon powder particle that hydrogenation gas carries can make gravity open valve 18 open automatically after separator 3 bottoms run up to certainweight, silica flour falls into conversion zone 1 and reacts, and gravity open valve 18 is just closed automatically.This gravity open valve 18 can be to utilize spring to connect valve and realize.Maintenance end socket 8 lower ends also are provided with slag-drip opening 19, and reacted residue is discharged by slag-drip opening 19.
Adopt ebullated bed reactor of the present utility model,, the hydrogenization of silicon tetrachloride production technology improved a lot in following several respects by the above technical process hydrogenization of silicon tetrachloride:
1, a gas distribution dish 7 is more evenly distributed gas mixture with secondary air distributing disc 6 in reactor, especially the uniformity coefficient of 6 pairs of gas fields of secondary air distributing disc has very big influence, further, the pattern of pipe cap 12 has very big influence to the uniformity coefficient and the distribution range of gas field, and described pipe cap 12 can change the flow direction of gas field with patterns such as pipe or plates.To sum up, 6 pairs of gas fluidized quality of ebullated bed of gas distribution dish improve a lot.
2, separator 3 has reduced the silica flour carrying rate of hydrogenation gas to a great extent, the loss of material and the difficulty that hydrogenation gas later separation is purified have further been reduced, make material to finish and participate in reaction fully, improved material and made full use of rate, increased substantially throughput.
3, the hydrogenization of silicon tetrachloride ebullated bed is simple in structure, and is easy and simple to handle, and throughput, reaction efficiency and utilization of materials are improved greatly, for polysilicon industry processing silicon chloride provides very big efficient and income, is a big new bright spot in the polysilicon industry.
Claims (9)
1. hydrogenization of silicon tetrachloride ebullated bed reactor, include the conversion zone (1), expanding reach (2) and the segregation section that link successively from bottom to top, also be equiped with material inlet (5) and hydrogenation gas outlet (4) in the top of described reactor, described segregation section (3) is equiped with the separator (3) that links with described hydrogenation gas outlet (4) bottom; Also be equiped with maintenance end socket (8) in the bottom of described reactor, be equiped with combi inlet port (9) and slag-drip opening (19) on this maintenance end socket (8); It is characterized in that: between described maintenance end socket (8) and conversion zone (1), be equiped with a gas distribution dish (7) and secondary air distributing disc (6) from bottom to top successively.
2. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 1, it is characterized in that: a described gas distribution dish (7) is connected with described combi inlet port (9), and this gas distribution dish (7) also is connected by the outside peripheral tube (21) of an airway (20) and a gas distribution dish (7).
3. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 2 is characterized in that: described peripheral tube (21) ringwise, rich font or Polygons.
4. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 3 is characterized in that: evenly be laid with through hole (22) in the bottom of described peripheral tube (21).
5. according to claim 1,2,3 or 4 described hydrogenization of silicon tetrachloride ebullated bed reactors, it is characterized in that: described secondary air distributing disc (6) includes gas distribution grid (10), the pipe cap (12) that is equiped with axial thread through hole (11) and links with described tapped through hole (11) on described gas distribution grid (10).
6. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 5, it is characterized in that: described pipe cap (12) is convexly set in described gas distribution grid (10), the periphery at itself and described gas distribution grid (10) place of linking be provided with the threaded portion in order to the tapped through hole (11) of described gas distribution grid (10) with thread connection.
7. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 6, it is characterized in that: be provided with axial ventilating pit (13) in the described pipe cap (12), the lower end of this axial ventilating pit (13) is connected with the bottom of described gas distribution grid (10), the upper end closed of this axial ventilating pit (13).
8. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 6, it is characterized in that: described pipe cap (12) also is equiped with radially ventilating pit (14), and it evenly is laid in the sidewall of described axial ventilating pit (13) or end and is connected with the top of described gas distribution grid (10).
9. hydrogenization of silicon tetrachloride ebullated bed reactor according to claim 1, it is characterized in that: the upper end of described separator (3) is provided with separator tangential inlet (16) in tangential direction, the bottom of described separator (3) is equiped with tapered separator awl section (17), is equiped with gravity open valve (18) in the bottom of this separator awl section (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202739629U CN201605166U (en) | 2009-11-27 | 2009-11-27 | Hydrogenation silicon tetrachloride boiling bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202739629U CN201605166U (en) | 2009-11-27 | 2009-11-27 | Hydrogenation silicon tetrachloride boiling bed reactor |
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| Publication Number | Publication Date |
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| CN201605166U true CN201605166U (en) | 2010-10-13 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2009202739629U Expired - Lifetime CN201605166U (en) | 2009-11-27 | 2009-11-27 | Hydrogenation silicon tetrachloride boiling bed reactor |
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| CN (1) | CN201605166U (en) |
Cited By (3)
| 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 |
| CN107224941A (en) * | 2017-06-26 | 2017-10-03 | 辽宁加宝石化设备有限公司 | A kind of low pressure drop high stability distributor and reactor |
| EP4212238A4 (en) * | 2021-11-18 | 2023-09-27 | Lg Chem, Ltd. | Sparger and reactor comprising same |
-
2009
- 2009-11-27 CN CN2009202739629U patent/CN201605166U/en not_active Expired - Lifetime
Cited By (3)
| 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 |
| CN107224941A (en) * | 2017-06-26 | 2017-10-03 | 辽宁加宝石化设备有限公司 | A kind of low pressure drop high stability distributor and reactor |
| EP4212238A4 (en) * | 2021-11-18 | 2023-09-27 | Lg Chem, Ltd. | Sparger and reactor comprising same |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI MORIMATSU CHEMICAL EQUIPMENT CO., LTD. Free format text: FORMER OWNER: SHANGHAI SENHE INVESTMENT CO., LTD. Effective date: 20110412 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 200240 ROOM 619, BUILDING 5, NO. 951, JIANCHUAN ROAD, MINHANG DISTRICT, SHANGHAI TO: 201323 NO. 29, JINWEN ROAD, ZHUQIAO INDUSTRIAL AREA, NANHUI DISTRICT, SHANGHAI |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20110412 Address after: Nanhui District 201323 Shanghai Zhu Bridge Industrial Zone gold smell Road No. 29 Patentee after: Shanghai Morimatsu Chemical Equipment Co., Ltd. Address before: 200240 Shanghai city Minhang District Jianchuan Road No. 951 Building 5 room 619 Patentee before: Shanghai Senhe Investment Co., Ltd. |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20101013 Effective date of abandoning: 20091127 |