CN214880245U - Synthesizer of silicon tetrachloride - Google Patents
Synthesizer of silicon tetrachloride Download PDFInfo
- Publication number
- CN214880245U CN214880245U CN202120239431.9U CN202120239431U CN214880245U CN 214880245 U CN214880245 U CN 214880245U CN 202120239431 U CN202120239431 U CN 202120239431U CN 214880245 U CN214880245 U CN 214880245U
- Authority
- CN
- China
- Prior art keywords
- silicon tetrachloride
- storage tank
- fluidized bed
- condenser
- steam generator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Silicon Compounds (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model belongs to the technical field of the chemical industry, in particular to synthesizer of silicon tetrachloride, liquid chlorine storage tank delivers to liquid chlorine vaporizer through the canned pump with liquid chlorine, chlorine after the gasification is converged with hydrogen chloride and is let in fluidized bed reactor, the silica flour storage tank delivers to fluidized bed reactor through nitrogen with silica flour through the metering tank, synthetic gas removes dust through cyclone and sack cleaner after steam generator one and delivers to first condenser, it gets back to fluidized bed reactor and continues the reaction to subside silica flour, the liquid phase silicon tetrachloride of condensation is delivered to the silicon tetrachloride storage tank, gaseous phase trichlorosilane is delivered to photocatalytic reactor, photocatalytic reactor lets in chlorine and hydrogen reaction secondary generation silicon tetrachloride, give vent to anger and deliver to the second condenser after steam generator two, the liquid phase silicon tetrachloride of formation is delivered to the silicon tetrachloride storage tank, hydrogen chloride and hydrogen are got back to photocatalytic reactor and continue the reaction. The synthesis device improves the conversion rate of the silicon tetrachloride, improves the energy utilization rate and reduces the production cost on the premise of not improving the requirement of equipment.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, in particular to synthesizer of silicon tetrachloride.
Background
Silicon tetrachloride is an important chemical product, is decomposed and releases heat when being heated or meeting water, emits corrosive smoke, is corrosive to a plurality of metals, particularly humid air, and has asphyxiating odor. Silicon tetrachloride can be used as a synthetic raw material for fine silicon dioxide, synthetic quartz, silicon nitride and other various organic silicon compounds, such as silicates, organic silicon monomers, organic silicon oil, high-temperature insulating paint, organic silicon resin, silicon rubber and heat-resistant lining materials. Silicon powder is often industrially synthesized into silicon tetrachloride by directly reacting with hydrogen chloride at high temperature, and a fluidized bed reactor is adopted in the reaction part of the method. In order to improve the conversion rate of the silicon tetrachloride, the temperature of the fluidized bed reactor is required to be increased to more than 800 ℃, the conversion rate of the silicon tetrachloride is 70-80% and the conversion rate of the trichlorosilane is 20-30%, and although the temperature is increased, the conversion rate of the silicon tetrachloride is still not high, and the requirement of high temperature on equipment is strict. In order to keep the temperature range of the reactor, a common heat taking mode is to add a large amount of nitrogen or chlorine to increase the excessive amount of nitrogen or chlorine to be used as a refrigerant to remove the heat generated by the reaction, and to take away the heat generated in the reaction process by using the nitrogen or chlorine, the part of heat cannot be recovered, so that the production resource consumption cost is increased, the requirement on equipment is high, the equipment acquisition cost is increased, and the potential safety hazard and the energy waste are also caused.
SUMMERY OF THE UTILITY MODEL
In view of the above situation, the utility model designs a synthesizer of silicon tetrachloride.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a silicon tetrachloride synthesis device comprises a liquid chlorine storage tank, a silicon powder storage tank, a fluidized bed reactor, a shield pump, a liquid chlorine gasifier, a metering tank, a first steam generator, a second steam generator, a cyclone dust collector, a bag-type dust collector, a photocatalytic reactor, a first condenser, a second condenser and a silicon tetrachloride storage tank, wherein a discharge port of the liquid chlorine storage tank is connected to the liquid chlorine gasifier through the shield pump, a gas outlet of the liquid chlorine gasifier is connected to a chlorine gas inlet at the bottom of the fluidized bed reactor, a hydrogen chloride gas inlet is further arranged at the bottom of the fluidized bed reactor, a discharge port of the silicon powder storage tank is connected to a silicon powder feed inlet of the fluidized bed reactor through the metering tank, a heat conduction oil inlet and a heat conduction oil outlet are further arranged on the fluidized bed reactor, a gas outlet at the top of the fluidized bed reactor is connected to the gas inlet of the first steam generator, a gas outlet of the first steam generator is connected to the gas inlet of the cyclone dust collector, the gas outlet of cyclone is connected to the sack cleaner, the discharge gate of sack cleaner and cyclone bottom all is connected to fluidized bed reactor's returning charge mouth, the gas outlet of sack cleaner is connected to the air inlet of first condenser, the liquid outlet of first condenser is connected to the silicon tetrachloride storage tank, the gas outlet of first condenser is connected to photocatalytic reactor's trichlorosilane feed inlet, photocatalytic reactor bottom still is provided with chlorine import and hydrogen import, last steam inlet and the steam outlet of still being provided with of photocatalytic reactor, the gas outlet at photocatalytic reactor top is connected to the air inlet of steam generator two, the gas outlet of steam generator two is connected to the air inlet of second condenser, the liquid outlet of second condenser is connected to the silicon tetrachloride storage tank, the gas outlet of second condenser is connected to photocatalytic reactor's returning charge mouth.
Furthermore, water inlets of the first steam generator and the second steam generator are connected to a deionized water pipeline, and steam generated by heat exchange can be used for heating the liquid chlorine gasifier and the photocatalytic reactor.
Furthermore, a steam heating port and a condensed water outlet are arranged on the liquid chlorine gasifier.
Further, the bag-type dust collector is a pulse back-blowing bag-type dust collector.
The utility model discloses still including other subassemblies that can make its normal use, be the conventional means in this field, in addition, the utility model discloses in add the device or the subassembly of injecing, all adopt the prior art in this field, for example: a shield pump, a liquid chlorine gasifier, a metering tank, a fluidized bed reactor, a photocatalytic reactor, a cyclone dust collector, a steam generator, a condenser and the like.
The utility model has the advantages as follows:
the utility model provides a synthesizer of silicon tetrachloride adopts fluidized bed reactor to add twice reaction of photocatalytic reactor again for silicon tetrachloride's conversion rate can reach 95-98%, need not to promote under the prerequisite of reacting equipment's high temperature resistant and high pressure resistant requirement, the conversion rate of silicon tetrachloride has been improved remarkably, the security of production has been improved, the thermal recovery of reaction is recycled in addition, the utilization ratio of the energy has been improved, when having promoted production efficiency, production cost is reduced, the economic benefits of enterprise has been improved.
Drawings
FIG. 1 is a schematic structural diagram of a synthesis apparatus in the example.
Detailed Description
The technical solution of the present invention will be described more clearly and completely with reference to specific embodiments, and it should be understood that the described embodiments are only some embodiments of the present invention, not all embodiments.
Examples
As shown in figure 1, the silicon tetrachloride synthesis device comprises a liquid chlorine storage tank 1, a silicon powder storage tank 2, a fluidized bed reactor 3, a shielding pump 4, a liquid chlorine gasifier 5, a metering tank 6, a first steam generator 7, a second steam generator 8, a cyclone dust collector 9, a bag-type dust collector 10, a photocatalytic reactor 11, a first condenser 12, a second condenser 13 and a silicon tetrachloride storage tank 14, wherein a discharge port of the liquid chlorine storage tank is connected to the liquid chlorine gasifier through the shielding pump, a gas outlet of the liquid chlorine gasifier is connected to a chlorine gas inlet at the bottom of the fluidized bed reactor, a hydrogen chloride gas inlet is further arranged at the bottom of the fluidized bed reactor, a discharge port of the silicon powder storage tank is connected to a silicon powder feed inlet of the fluidized bed reactor through the metering tank, a heat-conducting oil inlet and a heat-conducting oil outlet are further arranged on the fluidized bed reactor, a gas outlet at the top of the fluidized bed reactor is connected to a gas inlet of the first steam generator, the gas outlet of steam generator I is connected to cyclone's air inlet, cyclone's gas outlet is connected to the sack cleaner, the discharge gate of sack cleaner and cyclone bottom all is connected to fluidized bed reactor's returning charge mouth, the gas outlet of sack cleaner is connected to the air inlet of first condenser, the liquid outlet of first condenser is connected to the silicon tetrachloride storage tank, the gas outlet of first condenser is connected to photocatalytic reactor's trichlorosilane feed inlet, photocatalytic reactor bottom still is provided with chlorine import and hydrogen import, still be provided with steam inlet and steam outlet on the photocatalytic reactor, the gas outlet at photocatalytic reactor top is connected to the air inlet of steam generator two, the gas outlet of steam generator two is connected to the air inlet of second condenser, the liquid outlet of second condenser is connected to the silicon tetrachloride storage tank, the gas outlet of second condenser is connected to photocatalytic reactor's returning charge mouth.
The water inlets of the first steam generator and the second steam generator are connected to a deionized water pipeline, steam generated by heat exchange can be used for heating the liquid chlorine gasifier and the photocatalytic reactor, the liquid chlorine gasifier and other equipment of the production system can also be used for heating, and the deionized water can effectively prevent pipelines and equipment from scaling.
And the liquid chlorine gasifier is provided with a steam heating port and a condensed water outlet.
The bag-type dust collector is a pulse back-blowing bag-type dust collector.
The method comprises the steps that liquid chlorine is conveyed to a liquid chlorine gasifier through a discharge port of a liquid chlorine storage tank through a shielding pump, gasified chlorine and externally-connected hydrogen chloride gas are introduced into the bottom of a fluidized bed reactor, the fluidized bed reactor is heated to 200-340 ℃ by utilizing heat conduction oil, a discharge port of a silicon powder storage tank is connected to a metering tank, nitrogen is introduced into the top of the metering tank, silicon powder enters the fluidized bed reactor under the carrying of the nitrogen after being metered, gas discharged from the top of the fluidized bed reactor is conveyed to a cyclone dust collector after first heat exchange through a steam generator, a gas outlet of the cyclone dust collector is connected to a bag-type dust collector, incompletely-reacted silicon powder settled from the bottoms of the cyclone dust collector and the bag-type dust collector returns to the fluidized bed reactor under the carrying of the nitrogen for continuous reaction, gas discharged from the bag-type dust collector is conveyed to a first condenser, liquid-phase silicon tetrachloride generated by condensation is conveyed to a silicon tetrachloride storage tank, and gas-phase trichlorosilane not condensed is conveyed to a photocatalytic reactor for continuous reaction, and heating the photocatalytic reactor to 120-180 ℃ by using steam, introducing chlorine and hydrogen into the bottom of the photocatalytic reactor to react with trichlorosilane under the irradiation of ultraviolet rays to generate silicon tetrachloride and hydrogen chloride, exchanging heat of the discharged gas of the photocatalytic reactor through a second steam generator, sending the gas to a second condenser, sending the condensed liquid-phase silicon tetrachloride to a silicon tetrachloride storage tank, and returning the uncondensed hydrogen chloride and hydrogen which are not completely reacted to the photocatalytic reactor to continue to react.
The fluidized bed reactor can also be added with CuCl2As the catalyst, the temperature and pressure conditions of the synthesis reaction can be reduced, the equipment requirement of the fluidized bed reactor is reduced, and the equipment manufacturing cost is reduced.
The mole ratio of chlorine to hydrogen introduced into the photocatalytic reactor is 2: 1-8: 1, the introduction amount of the chlorine is larger than that of the hydrogen, and the trichlorosilane and the chlorine are enabled to react more fully to generate the silicon tetrachloride.
The technical solution of the present invention is not limited to the above-mentioned specific embodiments, and many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.
Claims (4)
1. The utility model provides a synthesizer of silicon tetrachloride, includes liquid chlorine storage tank, silica flour storage tank and fluidized bed reactor, its characterized in that: the device also comprises a shielding pump, a liquid chlorine gasifier, a metering tank, a first steam generator, a second steam generator, a cyclone dust collector, a bag-type dust collector, a photocatalytic reactor, a first condenser, a second condenser and a silicon tetrachloride storage tank, wherein a discharge port of the liquid chlorine storage tank is connected to the liquid chlorine gasifier through the shielding pump, a gas outlet of the liquid chlorine gasifier is connected to a chlorine gas inlet at the bottom of the fluidized bed reactor, a hydrogen chloride gas inlet is also arranged at the bottom of the fluidized bed reactor, a discharge port of the silicon powder storage tank is connected to a silicon powder feed inlet of the fluidized bed reactor through the metering tank, a heat conduction oil inlet and a heat conduction oil outlet are also arranged on the fluidized bed reactor, a gas outlet at the top of the fluidized bed reactor is connected to a gas inlet of the first steam generator, a gas outlet of the first steam generator is connected to a gas inlet of the cyclone dust collector, and a gas outlet of the cyclone dust collector is connected to the bag-type dust collector, the discharge gate of sack cleaner and cyclone bottom all is connected to fluidized bed reactor's returning charge mouth, the gas outlet of sack cleaner is connected to the air inlet of first condenser, the liquid outlet of first condenser is connected to the silicon tetrachloride storage tank, the gas outlet of first condenser is connected to the trichlorosilane feed inlet of photocatalytic reactor, photocatalytic reactor bottom still is provided with chlorine import and hydrogen import, still be provided with steam inlet and steam outlet on the photocatalytic reactor, the gas outlet at photocatalytic reactor top is connected to the air inlet of steam generator two, the gas outlet of steam generator two is connected to the air inlet of second condenser, the liquid outlet of second condenser is connected to the silicon tetrachloride storage tank, the gas outlet of second condenser is connected to the returning charge mouth of photocatalytic reactor.
2. A silicon tetrachloride synthesis apparatus according to claim 1, characterized in that: and water inlets of the first steam generator and the second steam generator are connected to a deionized water pipeline, and steam generated by heat exchange can be used for heating the liquid chlorine gasifier and the photocatalytic reactor.
3. A silicon tetrachloride synthesis apparatus according to claim 2, characterized in that: and the liquid chlorine gasifier is provided with a steam heating port and a condensed water outlet.
4. A silicon tetrachloride synthesis apparatus according to claim 1, characterized in that: the bag-type dust collector is a pulse back-blowing bag-type dust collector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120239431.9U CN214880245U (en) | 2021-01-28 | 2021-01-28 | Synthesizer of silicon tetrachloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120239431.9U CN214880245U (en) | 2021-01-28 | 2021-01-28 | Synthesizer of silicon tetrachloride |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214880245U true CN214880245U (en) | 2021-11-26 |
Family
ID=78859827
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120239431.9U Active CN214880245U (en) | 2021-01-28 | 2021-01-28 | Synthesizer of silicon tetrachloride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214880245U (en) |
-
2021
- 2021-01-28 CN CN202120239431.9U patent/CN214880245U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101143723B (en) | Modified method and device for preparing trichlorosilane and multicrystal silicon | |
| CN101279735A (en) | Production method and apparatus for trichlorosilane | |
| CN100556507C (en) | A kind of method for recovering tail gas of trichlorosilane production | |
| CN102730691B (en) | Energy utilization in polysilicon hydrogenation process | |
| CN101492398B (en) | Urea production process of high-efficiency condensation, low-mounting height CO2 air stripping method and high-voltage lamp type full condensation reactor | |
| CN112647085B (en) | Method for synthesizing high-purity disilane through electrocatalysis | |
| CN101940898B (en) | Method for recycling silicon tetrachloride | |
| CN107158891A (en) | A kind of coal gasified black water flashed vapour utilizes technique | |
| CN214880245U (en) | Synthesizer of silicon tetrachloride | |
| CN102923716A (en) | Process for producing trichlorosilane through inverse disporportionation of dichlorosilane | |
| US6476262B2 (en) | Urea synthesis process and apparatus | |
| CN103449440B (en) | Equipment for preparing polycrystalline silicon | |
| CN201136791Y (en) | Device for conversing silicon tetrachloride to be trichlorosilane by hydrochlorination process | |
| CN215886877U (en) | Device for continuously producing alkyl orthosilicate from silicon powder | |
| CN217568762U (en) | Tower-type gas-liquid-phase chloroethylene production device | |
| CN103482630B (en) | Prepare the method for polysilicon | |
| CN109467091A (en) | A kind of energy saver and method of silicon tetrachloride synthesis | |
| CN112663074B (en) | System for synthesizing high-purity disilane through electrocatalysis | |
| CN201485289U (en) | Device utilizing silicon tetrachloride for producing trichlorosilane | |
| CN108689798A (en) | A method of improving organic silicon monomer synthesis recycling chloromethanes quality | |
| CN104725181B (en) | Initial separation technique of gas generated by reaction for preparing propylene from oxygen-containing compounds | |
| CN109456431B (en) | Clean closed-loop production method and system for polyolefin | |
| CN209722000U (en) | A kind of device for acetic acid ammonification synthesis acetonitrile | |
| EP3950593A1 (en) | Method for preparing ammonia by using ammonium salt and silicate | |
| CN107572534B (en) | A kind of technique and system preparing trichlorosilane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PP01 | Preservation of patent right | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20230710 Granted publication date: 20211126 |