CN201572633U - Fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production - Google Patents
Fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production Download PDFInfo
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- CN201572633U CN201572633U CN2009202560252U CN200920256025U CN201572633U CN 201572633 U CN201572633 U CN 201572633U CN 2009202560252 U CN2009202560252 U CN 2009202560252U CN 200920256025 U CN200920256025 U CN 200920256025U CN 201572633 U CN201572633 U CN 201572633U
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- fluidized bed
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Abstract
A fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production relates to a large-sized fluidized bed reactor in trichlorosilane production. The fluidized bed reactor comprises a gas-solid separation section, a reaction section and a seal head section which are mutually connected from top to bottom, the upper portion of the gas-solid separation section is provided with a synthetic gas outlet and a safety releasing opening, a heating device is arranged inside the reaction section, and a hydrogen chloride inlet is arranged on the seal head section. The fluidized bed reactor is characterized in that a gas distributor is arranged between the reaction section and the seal head section, air holes are uniformly arranged on the gas distributor, and each air hole is provided with a conical gas cap. The fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production is greatly improved on the basis of the existing fluidized bed reactor structure, and has the following obvious advantages that the gas distributor leads hydrogen chloride gas to uniformly enter the reaction section, thereby leading reaction to be more uniform, and increasing hydrogen chloride utilization and conversion rate of silica powder.
Description
Technical field
The utility model relates to a kind of equipment of chemical field, the large-scale fluidized bed reactor that particularly a kind of trichlorosilane is produced.
Trichlorosilane (HSiCl3) is a kind of purposes organic silicon monomer very widely, is mainly used in to produce semiconductor silicon, monocrystalline silicon and polysilicon, is widely used in the every field of national defence, national defence economy and even people's daily life.Trichlorosilane is still produced the important source material of silane coupler and other organo-silicon compound.In recent years, China is increasing to the demand of trichlorosilane.
Domestic existing trichlorosilane process units generally adopts the small-sized fluidized bed reactor.Its structure mostly is tubular greatly, and the upper diameter enlarged is the gas-solid section of being separated, and this section be high discharging opening, and the direct tube section at middle part is a conversion zone, conversion zone outsourcing heater, and top is provided with the silica flour charging aperture, and the bottom connects low head, and the hydrogen chloride air inlet is arranged on the low head.The major defect of its existence is: the silica flour amount and the hydrogen chloride gas scale of construction do not match, and the hydrogen chloride gas skewness causes that the silica flour conversion ratio is low, the hydrogen chloride utilization rate is low.
The utility model content
In order to solve above-mentioned technical problem, the purpose of this utility model is, the uniform trichlorosilane production of a kind of reaction large-scale fluidized bed reactor is provided.
To achieve these goals, the utility model is taked following technical scheme: the utility model comprises interconnective gas solid separation section, conversion zone and seal head section from top to bottom, gas solid separation section top is provided with forming gas outlet and safe release mouth, be provided with heater in the conversion zone, seal head section is provided with the hydrogen chloride air inlet, the conversion zone bottom is provided with the silica flour charging aperture, be provided with gas distributor between described conversion zone and the seal head section, be equipped with pore on the gas distributor, each pore is provided with the taper gas cap.
Further, described conversion zone bottom is provided with the silica flour charging aperture, and the ratio of the height of conversion zone and diameter is 2-10.
Further, described heater is the conduction oil heat-exchanging tube bundle that is arranged in the conversion zone, and the conduction oil heat-exchanging tube bundle extends heat conductive oil inlet and the outlet with the outer conduction oil connection of cylindrical shell outside cylindrical shell.
Further, described seal head section lower end is provided with slag-drip opening.
Further, described conduction oil tube bank is by way of complete section of conversion zone.
Trichlorosilane large-scale fluidized bed reactor of the present utility model, on existing fluidized-bed reactor structure, carried out big improvement, have following significant effect: the setting of gas distributor, hydrogen chloride gas is evenly entered in the conversion zone, make reaction more even.Improved the conversion ratio of hydrogen chloride utilization rate and silica flour.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
1-gas solid separation section, the outlet of 2-forming gas, 3-conversion zone, 4-conduction oil heat-exchanging tube bundle, 5-heat conductive oil inlet, the outlet of 6-conduction oil, 7-silica flour charging aperture, 8-low head, 9-hydrogen chloride air inlet, 10-slag-drip opening, 11-gas distributor, 12-taper gas cap, 13-safe release mouth.
The specific embodiment
Referring to Fig. 1, the large-scale trichlorosilane resultant current of the utility model fluidized bed reactor is a tubular construction, and top barrel diameter expanding reach is a gas solid separation section 1, and gas solid separation section 1 is a reverse frustoconic, this section is provided with safe release mouth 13 and forming gas outlet 2, and outlet 2 upwards helps discharging.
Conversion zone 3 bottoms connect low head 8, have hydrogen chloride air inlet 9 on the low head 8.Slag-drip opening 10 is arranged at low head 8 bottoms, and hydrogen chloride air inlet 9 tops are provided with gas distributor 11, are distributed with pore on the gas distributor 11, for increasing the distribution effect, taper gas cap 12 is housed on the pore of above-mentioned gas distributor 11.
In order better to improve the output of trichlorosilane, the utility model can further be taked following technical scheme on the basis of such scheme:
The direct tube section at middle part is a conversion zone 3, and the bottom of conversion zone 3 is provided with silica flour charging aperture 7, and the ratio of the height of conversion zone 3 and diameter is 2-10.
Be provided with conduction oil heat-exchanging tube bundle 4 in the conversion zone 3, this conduction oil heat-exchanging tube bundle 4 extends to conversion zone 3 bottoms from conversion zone 3 tops always, and conduction oil heat-exchanging tube bundle 4 is communicated with cylindrical shell heat conductive oil inlet 5 and outlet 6 outward;
Above-mentioned gas solid separation section 1, conversion zone 3, low head 8 connect by flange each other, are convenient to loading and unloading and maintenance.
On the pore of above-mentioned gas distributor 11 taper gas cap 12 is housed.Conversion zone 3, gas solid separation section 1, low head 8, gas distributor 11 are absolute construction, and parts connect by flange each other.The diameter of gas solid separation section 1 is 2000-3500mm.The diameter of conversion zone 3 is 1000-2000mm.Conversion zone 3 height are 2-10 with the ratio of conversion zone 3 diameters.Conduction oil heat-exchanging tube bundle 4 bottoms are 50-200mm apart from pore taper gas cap 12 distances of gas distributor 11.Silica flour charging aperture 7 is 250-2500mm apart from conversion zone 3 distances from bottom.Conduction oil heat-exchanging tube bundle 4 upper edges are 3500-10000mm apart from conversion zone 3 distances from bottom.
Adopt above-mentioned large-scale trichlorosilane resultant current fluidized bed reactor, following concrete steps are arranged, at first the levels of metal silica flour is joined 3500-10000mm height in the fluid bed, start the heat-conducting oil heating pattern, fluidized-bed temperature is heated to 250-350 ℃, feeds hydrogen chloride gas simultaneously, treat silica flour and hydrogen chloride gas begin the reaction after, start the conduction oil refrigerating mode reaction heat is shifted out, effectively control reaction temperature by the amount of regulating conduction oil.
Claims (5)
1. trichlorosilane fluidized-bed reactor, comprise interconnective gas solid separation section, conversion zone and seal head section from top to bottom, gas solid separation section top is provided with forming gas outlet and safe release mouth, be provided with heater in the conversion zone, seal head section is provided with the hydrogen chloride air inlet, it is characterized in that, is provided with gas distributor between described conversion zone and the seal head section, be equipped with pore on the gas distributor, each pore is provided with the taper gas cap.
2. trichlorosilane fluidized-bed reactor according to claim 1 is characterized in that, described conversion zone bottom is provided with the silica flour charging aperture, and the ratio of the height of conversion zone and diameter is 2-10.
3. trichlorosilane fluidized-bed reactor according to claim 1, it is characterized in that, described heater is the conduction oil heat-exchanging tube bundle that is arranged in the conversion zone, and the conduction oil heat-exchanging tube bundle extends heat conductive oil inlet and the outlet with the outer conduction oil connection of cylindrical shell outside cylindrical shell.
4. tri-chlorination hydrogen fluidized-bed reactor according to claim 1 is characterized in that described seal head section lower end is provided with slag-drip opening.
5. trichlorosilane fluidized-bed reactor according to claim 3 is characterized in that, described conduction oil tube bank is by way of complete section of conversion zone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202560252U CN201572633U (en) | 2009-12-01 | 2009-12-01 | Fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202560252U CN201572633U (en) | 2009-12-01 | 2009-12-01 | Fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201572633U true CN201572633U (en) | 2010-09-08 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202560252U Expired - Fee Related CN201572633U (en) | 2009-12-01 | 2009-12-01 | Fluidized bed reactor for increasing reaction uniformity degree in trichlorosilane production |
Country Status (1)
| Country | Link |
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| CN (1) | CN201572633U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109317060A (en) * | 2018-12-06 | 2019-02-12 | 江苏新河农用化工有限公司 | A kind of fluidized bed distributor for Bravo production |
| CN109879289A (en) * | 2019-04-12 | 2019-06-14 | 四川永祥多晶硅有限公司 | A kind of low value silicon powder recycling system |
-
2009
- 2009-12-01 CN CN2009202560252U patent/CN201572633U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109317060A (en) * | 2018-12-06 | 2019-02-12 | 江苏新河农用化工有限公司 | A kind of fluidized bed distributor for Bravo production |
| CN109879289A (en) * | 2019-04-12 | 2019-06-14 | 四川永祥多晶硅有限公司 | A kind of low value silicon powder recycling system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100908 Termination date: 20121201 |