CN203529947U - Silicon powder recovery device for producing silicon tetrachloride by adopting direct method - Google Patents
Silicon powder recovery device for producing silicon tetrachloride by adopting direct method Download PDFInfo
- Publication number
- CN203529947U CN203529947U CN201320699127.8U CN201320699127U CN203529947U CN 203529947 U CN203529947 U CN 203529947U CN 201320699127 U CN201320699127 U CN 201320699127U CN 203529947 U CN203529947 U CN 203529947U
- Authority
- CN
- China
- Prior art keywords
- silicon tetrachloride
- cyclone
- direct method
- outlet
- cyclone separator
- 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.)
- Expired - Lifetime
Links
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 239000005049 silicon tetrachloride Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 27
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 title abstract description 11
- 238000011084 recovery Methods 0.000 title abstract description 4
- 239000011863 silicon-based powder Substances 0.000 title abstract 5
- 239000000428 dust Substances 0.000 claims abstract description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 66
- 239000000377 silicon dioxide Substances 0.000 claims description 33
- 239000004744 fabric Substances 0.000 claims description 25
- 239000000835 fiber Substances 0.000 claims description 22
- 239000012716 precipitator Substances 0.000 claims description 21
- 239000000843 powder Substances 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 17
- 239000010881 fly ash Substances 0.000 claims description 12
- 239000003921 oil Substances 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 238000001514 detection method Methods 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 6
- 229910052593 corundum Inorganic materials 0.000 claims description 2
- 239000010431 corundum Substances 0.000 claims description 2
- 239000012043 crude product Substances 0.000 abstract description 22
- 239000002994 raw material Substances 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 18
- 235000013312 flour Nutrition 0.000 description 15
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 12
- 229910052801 chlorine Inorganic materials 0.000 description 12
- 239000000460 chlorine Substances 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 12
- 239000007921 spray Substances 0.000 description 12
- 239000007788 liquid Substances 0.000 description 10
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 235000012239 silicon dioxide Nutrition 0.000 description 5
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000005046 Chlorosilane Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 4
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 4
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- 229960001866 silicon dioxide Drugs 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- YGZSVWMBUCGDCV-UHFFFAOYSA-N chloro(methyl)silane Chemical compound C[SiH2]Cl YGZSVWMBUCGDCV-UHFFFAOYSA-N 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 3
- 229920005591 polysilicon Polymers 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 3
- 239000005052 trichlorosilane Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005660 chlorination reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- XHXFXVLFKHQFAL-UHFFFAOYSA-N phosphoryl trichloride Chemical compound ClP(Cl)(Cl)=O XHXFXVLFKHQFAL-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000002829 reductive effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 206010011906 Death Diseases 0.000 description 1
- 229910001021 Ferroalloy Inorganic materials 0.000 description 1
- 229910000519 Ferrosilicon Inorganic materials 0.000 description 1
- 229910000676 Si alloy Inorganic materials 0.000 description 1
- 229910003902 SiCl 4 Inorganic materials 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910021331 inorganic silicon compound Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021471 metal-silicon alloy Inorganic materials 0.000 description 1
- 150000001282 organosilanes Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 229920002545 silicone oil Polymers 0.000 description 1
- 229920002050 silicone resin Polymers 0.000 description 1
- 229920002379 silicone rubber Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- FAQYAMRNWDIXMY-UHFFFAOYSA-N trichloroborane Chemical compound ClB(Cl)Cl FAQYAMRNWDIXMY-UHFFFAOYSA-N 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Abstract
The utility model relates to a silicon powder recovery device for producing silicon tetrachloride by adopting a direct method. The silicon powder recovery device comprises a cyclone separating device and a bag-type dust collector, wherein the cyclone separating device comprises a primary cyclone separator and a secondary cyclone separator; a feed opening of the primary cyclone separator is connected with a fluidized bed reactor in which silicon tetrachloride is produced; the primary cyclone separator is connected with the secondary cyclone separator; the primary cyclone separator and the secondary cyclone separator are in backflow connection with the fluidized bed reactor respectively; a gas outlet in the upper part of the secondary cyclone separator is connected with the bag-type dust collector; the bag-type dust collector comprises an outer shell and a plurality of bag devices. Silicon powder in crude silicon tetrachloride gas produced in the fluidized bed reactor is subjected to two-stage dust collection through the cyclone separators, so that the most of silicon powder is recycled, the dust collection in the follow-up process is avoided, in addition, the utilization efficiency of raw materials is improved, and the selectivity of silicon tetrachloride in the crude product is more than 95%.
Description
Technical field
The utility model belongs to organosilane monomer synthesis technical field, relates in particular to the silica powder recovering device that a kind of direct method is produced silicon tetrachloride.
Background technology
Silicon tetrachloride, molecular formula: SiCl
4, for colourless, be corrosive, non-combustible liquid, have suffocative stink.While being exposed to wet air, form dense smoke, hydrogenchloride is emitted in hydrolysis rapidly.57.6 ℃ of boiling points.Fusing point-70.0 ℃.Can be used for manufacturing silicoorganic compound, as thermal silica, tetraethoxy, organic silicone oil, high-temperature insulation paint, silicone resin, silicon rubber and heat resistant pad lining material.High purity silicon tetrachloride is for manufacturing the material of polysilicon, high-purity silicon dioxide and inorganic silicon compound, silica fiber, and war industry is for the manufacture of NC mixture, and metallurgical industry is for the manufacture of corrosion-resistant ferrosilicon, and foundary industry is used as releasing agent etc.At present, the impact of photovoltaic industry external owing to being subject to " two anti-", almost in the situation of being annihilated, the raw material trichlorosilane device of polysilicon, also almost in full end-of-life state, only has few device to move in carry-deficit, and this has just caused the silicon tetrachloride as by-product of this industry fewer and feweri, silicon tetrachloride becomes tight pin product by the by product of giving it up, price, from freely, increases to more than 4000 yuan/ton, and also can't buy on market.
Publication number be the Chinese patent of CN102712485A disclose a kind of by organic compound combustion generate electricity ash that manufacture technique produces, preferably organic compound combustion is converted to ignition energy under the existence of the grey carbonaceous material that the generating set of electric power produces to the method for the silicon-containing material chlorination production silicon tetrachloride that by silicon-containing material, preferably contains silicic acid biomass.Publication number is that the Chinese patent of CN102686514A also discloses a kind of granulation body and chlorine, oxygen that utilizes silicon-dioxide and carbonaceous material to form and carries out common chlorination reaction, generate the chlorinating step of silicon tetrachloride, and then silicon tetrachloride is generated to polysilicon with reductive agent metallic reducing.It is a kind of by the mixture of fine and/or unbodied silicon-dioxide, carbon and energy donor being changed to manufacture with chlorine the method for silicon tetrachloride that publication number is that the Chinese patent of CN101472839 also discloses.Energy donor is Pure Silicon Metal or silicon alloy, and the interpolation of donor has realized the thermopositive reaction of self-supporting on the one hand, has caused on the other hand showing of reacting initial temperature to be reduced.
Patent USP4490344, USP4604272, USP4847059, DE3438444/A1 and EP00077138 are by adding the mode of catalyzer, reduce chlorine, silicon-dioxide and carbon reaction and produce the method for the temperature of silicon tetrachloride, main group and the chlorine-containing compound of subgroup, preferably boron trichloride and phosphoryl chloride etc. that the catalyzer using is the periodic table of elements the 5th.
Publication number is that the Chinese patent of CN1114559C discloses and a kind ofly by by least having the chlorosilane of a HSi key in silicon, ferro-alloy metal or molecule, reacts under catalyst action with hydrogenchloride, thereby highly selective is produced the method for silicon tetrachloride.The utility model provides a kind of catalyzer of manufacturing the method for silicon tetrachloride comprise at least one periodictable VIII family's metallic element or its compound and be a kind ofly selected from periodictable VB family's period 3 and under the mixture of the element simple substance in cycle exists subsequently, make at least to have in silicon metal or molecule chlorosilane and the hcl reaction of a HSi key.USP3754077, USP4130632 disclose a kind of silicon, aluminium alloy and hydrogenchloride or chlorine gas of utilizing and have reacted, and generate the method for trichlorosilane or silicon tetrachloride.USP4980143 has introduced a kind of reaction with silica flour at hydrogenchloride in the process that generates trichlorosilane and silicon tetrachloride mixture, by changing the reaction conditionss such as temperature, can improve the content of silicon tetrachloride in mixed chlorosilane.Owing to there are a plurality of chlorosilane components in reaction process in these, later separation purifying process step is comparatively loaded down with trivial details.
The people such as the Fu Xuehong (research of the synthetic silicon tetrachloride of abandoned catalyst in direct synthesis methylchlorosilane, organosilicon material, 2011, 25(6): 397-401, the 13 Chinese organosilicon seminar collection of thesis in 2006), Yan Shicheng (the research of the synthetic silicon tetrachloride new technology of abandoned catalyst in direct synthesis methylchlorosilane, Northeast Electric Power University's journal, 2010, 30(6): 36-39.) Chinese patent CN1465524A etc. has introduced with (75% the Si of the waste catalyst in methyl chlorosilane monomer production process, 10 ~ 15% Cu) be main raw material, in the fluidized-bed reactor that is 600mm at diameter, synthesize the method for silicon tetrachloride with chlorine generation gas-solid reaction.
Applicant has applied for Chinese invention patent (number of patent application: 2013103609093, patent application day: 2013-8-19) disclose a kind of production equipment that utilizes direct method to produce silicon tetrachloride, this device comprises chlorine generating unit, silica flour feeding device, fluidized-bed reactor, cyclone separator, fiber bag precipitator, spray column and soda-wash tower, chlorine generating unit connects the inlet mouth of fluidized-bed reactor, silica flour feeding device connects the charging opening of fluidized-bed reactor, the skin of fluidized-bed reactor is provided with heating jacket, the air outlet on fluidized-bed reactor top is connected with interchanger, the discharge port of interchanger connects cyclone separator, the discharge gate of cyclone separator bottom refluxes respectively and is connected to described fluidized-bed reactor, the air outlet on cyclone separator top connects described fiber bag precipitator, the air outlet on fiber bag precipitator top connects described spray column, the air outlet on spray column top is connected with condenser, the discharge port of condenser is connected with silicon tetrachloride crude product storage tank, described silicon tetrachloride crude product storage tank connects described rectifier unit, the air outlet of described condenser connects described soda-wash tower.
Summary of the invention
The purpose of this utility model is to provide the silica powder recovering device that a kind of direct method is produced silicon tetrachloride, and this device is recycled silica flour in silicon tetrachloride crude product gas effectively, improves the prepared using efficiency of knowing clearly.
In order to realize above-mentioned object, the utility model has adopted following technical scheme:
A kind of direct method is produced the silica powder recovering device of silicon tetrachloride, this device comprises cyclone separator and fiber bag precipitator, described cyclone separator comprises primary cyclone and secondary cyclone, the opening for feed of primary cyclone connects the fluidized-bed reactor of producing silicon tetrachloride, the air outlet on primary cyclone top connects described secondary cyclone, the discharge gate of primary cyclone and secondary cyclone bottom refluxes respectively and is connected to described fluidized-bed reactor, the air outlet on secondary cyclone top connects described fiber bag precipitator, described fiber bag precipitator comprises body skin and a plurality of cloth bag device, in body skin, be provided with dividing plate, dividing plate is divided into dedusting chamber and outlet chamber by body skin, outer side wall in dedusting chamber is provided with heating jacket, and above dedusting chamber, be provided with fly-ash separator inlet mouth, fly-ash separator inlet mouth connects the air outlet on secondary cyclone top, in dedusting chamber, the inner side of fly-ash separator inlet mouth, is provided with gas block panel, described a plurality of cloth bag devices all adopt high temperature resistant material, and cloth bag device is fixedly installed on dividing plate, and dust outlet is set in the bottom in dedusting chamber, and dust outlet below is provided with fine powder withdrawing can, and the sidewall of described outlet chamber is provided with fly-ash separator air outlet.
As preferably, the fixedly inwall of described primary cyclone and secondary cyclone is provided with hexsteel, is lined with corundum in hexsteel.
As preferably, described fiber bag precipitator is also connected with cloth bag pulsed dust-removing device, cloth bag pulsed dust-removing device comprises compressed air tank, a plurality of Venturi meter, pulse control instrument and a plurality of pulse valve, described a plurality of pulse valves are arranged on a plurality of pipelines that are connected to compressed air tank and by pulse control instrument, are controlled respectively, a plurality of Venturi meters connect described a plurality of pipelines, and the air outlet of a plurality of Venturi meters is connected respectively to the inside of described cloth bag device.
As preferably, described fiber bag precipitator is also provided with pressure detection module, and described pressure detection module is connected with pulse control instrument.
As preferably, described heating jacket adopts heat-conducting oil heating, on the top of heating jacket, is provided with oil-in, and bottom is provided with oil outlet.
As preferably, the top in described dedusting chamber is right cylinder, and bottom is cone, at the outer side wall of cone, is provided with access hole.
The utility model is owing to having adopted above-mentioned technical scheme, the two-stage dedusting of the cyclone separator that the silica flour of the silicon tetrachloride crude product gas of producing for fluidized-bed reactor first passes through, most silica flour is recycled, how for thinner silica flour a small amount of in gas crude product, by sack cleaner, to reclaim, like this can most of silica flour of removing silicon tetrachloride crude product gas, avoided carrying out in subsequent technique dedusting, improved prepared using efficiency high, in crude product, silicon tetrachloride selectivity is more than 95% simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model silicon tetrachloride production equipment.
Fig. 2 is the structural representation of cyclone separator.
Fig. 3 is the vertical view of Fig. 2.
Fig. 4 is the structural representation of sack cleaner.
Fig. 5 is the vertical view of Fig. 4.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is made a detailed explanation.
A kind of production equipment that utilizes direct method to produce silicon tetrachloride as shown in Figure 1, this device comprises liquid chlorine storage tank 1, chlorine liquid carburetor 3, silica flour feeding device 5, fluidized-bed reactor 6, primary cyclone 10, secondary cyclone 11, fiber bag precipitator 12, spray column 14, soda-wash tower 18 etc.Wherein between the entrance of the outlet of liquid chlorine storage tank 1 and chlorine liquid carburetor 3, with canned-motor pump 2, be connected, be convenient to carrying out continuously of reaction.Between chlorine liquid carburetor 3 and fluidized-bed reactor 6, be connected with vacuum buffer tank 4, be convenient to stable being passed in fluidized-bed reactor 6 of gas velocity of the chlorine after vaporization.Described silica flour feeding device 5 is connected with nitrogen pipeline 21 above, and nitrogen pipeline 21 is provided with valve, by valve, is controlled and continuously silica flour is added to fluidized-bed reactor 6 bottoms.Fluidized-bed reactor adopts the heating jacket of oil bath heating, and heating jacket is provided with thermal oil entrance 8 and thermal oil outlet 7.The air outlet on fluidized-bed reactor 6 tops is connected with interchanger 9, and the discharge port of interchanger 9 connects described primary cyclone 10.As shown in Figure 2 and Figure 3, the air outlet on primary cyclone 10 tops connects described secondary cyclone 11, and the discharge gate of primary cyclone 10 and secondary cyclone 11 bottoms refluxes respectively and is connected to described fluidized-bed reactor 6.Fluidized-bed reactor 6 outlet products are after interchanger 9 coolings, gas crude product is after primary cyclone 10 is separated with secondary cyclone 11, and the most of solid fine silica powder in gas crude product reclaims to enter in fluidized-bed reactor 6 and continues as raw material reaction.The air outlet on described secondary cyclone 11 tops connects described fiber bag precipitator 12, the bottom of fiber bag precipitator 12 is connected with fine powder withdrawing can 13, makes thinner silica flour a small amount of in gas crude product by entering fine powder withdrawing can 13 after sack cleaner 12 recovery.Sack cleaner 12 outlet products enter spray column 14, the SiCl of spray liquid for using through the condensed partial reflux of condenser 16
4crude product, the air outlet on spray column 14 tops is connected with condenser 16, and the discharge port of condenser 16 connects branch line, and branch line one end is connected with silicon tetrachloride crude product storage tank 17, the other end connects the shower nozzle of described spray column 14, and spray column 14 bottoms are the high slag slurry storage tank 15 that boils of liquid.The SiCl of silicon tetrachloride crude product storage tank 17 for gathering
4crude product, can be used for further rectification and purification and uses.Condenser 16 unreacted is out chlorine gas mixture completely, generates the products such as clorox through soda-wash tower 18 with NaOH solution reaction, and product clorox enters clorox storage tank 19 and collects, and other noncondensable gas is discharged through drain 20.
As shown in Figure 4, described fiber bag precipitator 12 comprises body skin 21 and a plurality of cloth bag device 32, in body skin 21, be provided with dividing plate 22, dividing plate 22 is divided into dedusting chamber 23 and outlet chamber 24 by body skin 21, outer side wall in dedusting chamber 23 is provided with heating jacket 29, heating jacket 29 adopts heat-conducting oil heating, on the top of heating jacket 29, be provided with oil-in 30, bottom is provided with oil outlet 31, because silicon tetrachloride crude product gas is being lowered the temperature through primary cyclone 10 and secondary cyclone 11, if temperature is too low in fiber bag precipitator, can condense into liquid and stop up cloth bag device 32, therefore need to keep silicon tetrachloride crude product gas to mend by heating jacket 29 condenses.The top in dedusting chamber 23 is right cylinder, bottom is cone, the top in dedusting chamber 23 is provided with fly-ash separator inlet mouth 25, fly-ash separator inlet mouth 25 connects the air outlet on secondary cyclone 11 tops, in dedusting chamber, the inner side of fly-ash separator inlet mouth 25 23, be provided with gas block panel 36, at the outer side wall of cone, be provided with access hole 28.Described a plurality of cloth bag devices 32 all adopt high temperature resistant material, cloth bag device 32 is fixedly installed on dividing plate 22, dust outlet 27 is set in the bottom in dedusting chamber 23, and dust exports 27 belows and is provided with fine powder withdrawing can 13, and the sidewall of described outlet chamber 24 is provided with fly-ash separator air outlet 26.
As shown in Figure 5, described fiber bag precipitator 12 is also connected with cloth bag pulsed dust-removing device, cloth bag pulsed dust-removing device comprises compressed air tank 33, a plurality of Venturi meter 35, pulse control instrument and a plurality of pulse valve 34, described a plurality of pulse valves 34 are arranged on a plurality of pipelines that are connected to compressed air tank and by pulse control instrument, are controlled respectively, a plurality of Venturi meters 35 connect described a plurality of pipelines, and the air outlet of a plurality of Venturi meters 35 is connected respectively to the inside of described cloth bag device 32.And being also provided with pressure detection module at fiber bag precipitator 12, described pressure detection module is connected with pulse control instrument.In the process that dusty gas purifies by filter bag, along with the increase of time, the long-pending dust being attached on cloth bag device 32 is more and more, thereby the resistance of cloth bag device 32 is increased gradually, cause processing air quantity to reduce gradually, for normal work, control resistance within the specific limits, by pressure detection module, detect the pressure in fiber bag precipitator, at this moment when pressure is raised to limited range, by pulse control instrument, send instruction and trigger in order each control valve unbalanced pulse valve, pressurized air in gas bag is ejected in each corresponding cloth bag device 32 by each aperture Venturi meter 35 of injection tube, 32 moments of cloth bag device sharply expand, make the long-pending dust releasing that is attached to cloth bag device 32 surfaces, cloth bag device 32 is regenerated.
Principle of work of the present utility model is: the liquid chlorine in liquid chlorine storage tank 1 is input in chlorine liquid carburetor 3 and vaporizes to certain temperature through canned-motor pump 2, chlorine gas regulates laggard fluidized-bed reactor 6 bottoms that enter by surge tank 4, directly reacts in fluidized-bed reactor 6 with the raw material silica flour from silica flour feeding device 5.Fluidized-bed reactor 6 outlet crude products are after one-level cyclonic separation 10 is separated with secondary cyclone 11, and the most of solid fine silica powder in gas crude product reclaims to enter in fluidized-bed reactor 6 and continues as raw material reaction.In gas crude product, a small amount of thinner silica flour enters fine powder withdrawing can 13 after reclaiming by sack cleaner 12.Sack cleaner 12 outlet products enter spray column 14, the SiCl of spray liquid for using through the condensed partial reflux of condenser 16
4crude product, spray column 14 bottoms are the high slag slurry storage tank 15 that boils of liquid.The SiCl of storage tank 17 for gathering
4crude product, can be used for further rectification and purification and uses.Condenser 16 unreacted is out chlorine gas mixture completely, generates the products such as clorox through soda-wash tower 18 with NaOH solution reaction, and product clorox enters storage tank 19 and collects, and other noncondensable gas is discharged through drain 20.
Claims (6)
1. a direct method is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: this device comprises cyclone separator (10, 11) and fiber bag precipitator (12), described cyclone separator (10, 11) comprise primary cyclone (10) and secondary cyclone (11), the opening for feed of primary cyclone (10) connects the fluidized-bed reactor (6) of producing silicon tetrachloride, the air outlet on primary cyclone (10) top connects described secondary cyclone (11), the discharge gate of primary cyclone (10) and secondary cyclone (11) bottom refluxes respectively and is connected to described fluidized-bed reactor (6), the air outlet on secondary cyclone (11) top connects described fiber bag precipitator (12), described fiber bag precipitator (12) comprises body skin (21) and a plurality of cloth bag device (32), in body skin (21), be provided with dividing plate (22), dividing plate (22) is divided into dedusting chamber (23) and outlet chamber (24) by body skin (21), outer side wall in dedusting chamber (23) is provided with heating jacket (29), and be provided with fly-ash separator inlet mouth (25) in the top of dedusting chamber (23), fly-ash separator inlet mouth (25) connects the air outlet on secondary cyclone (11) top, in the dedusting chamber, inner side (23) of fly-ash separator inlet mouth (25), be provided with gas block panel (36), described a plurality of cloth bag devices (32) all adopt high temperature resistant material, cloth bag device (32) is fixedly installed on dividing plate (22), dust outlet (27) is set in the bottom of dedusting chamber (23), dust outlet (27) below is provided with fine powder withdrawing can (13), and the sidewall of described outlet chamber (24) is provided with fly-ash separator air outlet (26).
2. a kind of direct method according to claim 1 is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: the fixedly inwall of primary cyclone (10) and secondary cyclone (11) is provided with hexsteel, is lined with corundum in hexsteel.
3. a kind of direct method according to claim 1 is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: fiber bag precipitator (12) is also connected with cloth bag pulsed dust-removing device, cloth bag pulsed dust-removing device comprises compressed air tank (33), a plurality of Venturi meters (35), pulse control instrument and a plurality of pulse valve (34), described a plurality of pulse valves (34) are arranged on a plurality of pipelines that are connected to compressed air tank (33) and by pulse control instrument, are controlled respectively, a plurality of Venturi meters (35) connect described a plurality of pipelines, the air outlet of a plurality of Venturi meters (35) is connected respectively to the inside of described cloth bag device (32).
4. a kind of direct method according to claim 3 is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: fiber bag precipitator (12) is also provided with pressure detection module, and described pressure detection module is connected with pulse control instrument.
5. a kind of direct method according to claim 1 is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: heating jacket (29) adopts heat-conducting oil heating, on the top of heating jacket (29), be provided with oil-in (30), bottom is provided with oil outlet (31).
6. a kind of direct method according to claim 1 is produced the silica powder recovering device of silicon tetrachloride, it is characterized in that: the top of dedusting chamber (23) is right cylinder, and bottom is cone, at the outer side wall of cone, is provided with access hole (28).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320699127.8U CN203529947U (en) | 2013-11-06 | 2013-11-06 | Silicon powder recovery device for producing silicon tetrachloride by adopting direct method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320699127.8U CN203529947U (en) | 2013-11-06 | 2013-11-06 | Silicon powder recovery device for producing silicon tetrachloride by adopting direct method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203529947U true CN203529947U (en) | 2014-04-09 |
Family
ID=50416182
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320699127.8U Expired - Lifetime CN203529947U (en) | 2013-11-06 | 2013-11-06 | Silicon powder recovery device for producing silicon tetrachloride by adopting direct method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203529947U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103570025A (en) * | 2013-11-06 | 2014-02-12 | 浙江富士特集团有限公司 | Silicon powder recycling device for producing silicon tetrachloride through direct method |
| CN109847470A (en) * | 2019-01-31 | 2019-06-07 | 内蒙古通威高纯晶硅有限公司 | Cold hydrogenation silicon powder charging system emptying hydrogen recovery system and method |
| CN110694388A (en) * | 2019-11-12 | 2020-01-17 | 四川永祥新能源有限公司 | System for be arranged in getting rid of silica flour in tail gas |
-
2013
- 2013-11-06 CN CN201320699127.8U patent/CN203529947U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103570025A (en) * | 2013-11-06 | 2014-02-12 | 浙江富士特集团有限公司 | Silicon powder recycling device for producing silicon tetrachloride through direct method |
| CN103570025B (en) * | 2013-11-06 | 2016-01-13 | 浙江富士特集团有限公司 | A kind of direct method produces the silica powder recovering device of silicon tetrachloride |
| CN109847470A (en) * | 2019-01-31 | 2019-06-07 | 内蒙古通威高纯晶硅有限公司 | Cold hydrogenation silicon powder charging system emptying hydrogen recovery system and method |
| CN110694388A (en) * | 2019-11-12 | 2020-01-17 | 四川永祥新能源有限公司 | System for be arranged in getting rid of silica flour in tail gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101279735A (en) | Production method and apparatus for trichlorosilane | |
| CN103449445B (en) | A kind of direct method produces the production equipment of silicon tetrachloride | |
| CN102234117B (en) | A kind of method for hydrolysis of the material containing hydrolyzable halogen atom | |
| CN101143723A (en) | Modified method and device for preparing trichlorosilane and multicrystal silicon | |
| CN102849745B (en) | Dust removal process and system for trichlorosilane production | |
| CN100556507C (en) | A kind of method for recovering tail gas of trichlorosilane production | |
| CN203529947U (en) | Silicon powder recovery device for producing silicon tetrachloride by adopting direct method | |
| CN203568858U (en) | Production system for synthesis of silicon tetrachloride | |
| CN103566669A (en) | Bag type dust collector for producing silicon tetrachloride by direct method | |
| CN105540660A (en) | Production device for preparing ultra-pure zirconium oxychloride byproduct silicon tetrachloride by fluidizing chlorination of zircon sand | |
| CN105502491B (en) | The method that zircon sand fluidizing chlorination prepares ultrapure zirconium oxychloride by-produced tetrachlorosilane | |
| CN104925821B (en) | Production system for producing fumed silica by utilizing silicon tetrachloride | |
| CN102936014A (en) | Method and device for producing disilane through reaction of alloyed composition and ammonium chloride in liquid ammonia | |
| CN103382032A (en) | Preparation method for trichlorosilane from silicon tetrachloride | |
| CN107416841B (en) | Method and device for producing silicon tetrachloride | |
| CN103420382B (en) | A kind of synthetic method of silicon tetrachloride and production system thereof | |
| CN103570025B (en) | A kind of direct method produces the silica powder recovering device of silicon tetrachloride | |
| CN103553057B (en) | A kind of method utilizing reaction rectification technique process chlorosilane waste gas | |
| CN203451228U (en) | Production device for producing silicon tetrachloride by virtue of direct method | |
| CN204057977U (en) | For the apparatus system of halogen silicon polymer cracking for halosilanes | |
| CN103449440B (en) | Equipment for preparing polycrystalline silicon | |
| CN203507699U (en) | Cloth bag type dust collector for producing silicon tetrachloride by using direct method | |
| CN102219225B (en) | Device and method for recovering silicon dioxide after burning waste gas and waste liquid in polycrystalline silicon industry | |
| CN103482630B (en) | Prepare the method for polysilicon | |
| CN215886877U (en) | Device for continuously producing alkyl orthosilicate from silicon powder |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Liu Guojing Inventor after: Fang Weimin Inventor after: Tan Jun Inventor after: Wang Jianyang Inventor after: Qiu Xianhui Inventor before: Fang Weimin Inventor before: Tan Jun Inventor before: Liu Guojing Inventor before: Wang Jianyang Inventor before: Qiu Xianhui Inventor before: Liu Chengguo |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: FANG WEIMIN TAN JUN LIU GUOJING WANG JIANYANG QIU XIANHUI LIU CHENGGUO TO: LIU GUOJING FANG WEIMIN TAN JUN WANG JIANYANG QIU XIANHUI |
|
| CX01 | Expiry of patent term |
Granted publication date: 20140409 |
|
| CX01 | Expiry of patent term |