WO2023282136A1 - 一酸化珪素の製造方法 - Google Patents
一酸化珪素の製造方法 Download PDFInfo
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- WO2023282136A1 WO2023282136A1 PCT/JP2022/025890 JP2022025890W WO2023282136A1 WO 2023282136 A1 WO2023282136 A1 WO 2023282136A1 JP 2022025890 W JP2022025890 W JP 2022025890W WO 2023282136 A1 WO2023282136 A1 WO 2023282136A1
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- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Chemical compound [Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 0.000 title claims abstract description 292
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 142
- 239000000843 powder Substances 0.000 claims abstract description 74
- 239000011863 silicon-based powder Substances 0.000 claims abstract description 64
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 53
- 238000002485 combustion reaction Methods 0.000 claims abstract description 52
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910001882 dioxygen Inorganic materials 0.000 claims abstract description 50
- 239000011261 inert gas Substances 0.000 claims abstract description 37
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims abstract description 35
- 229910052710 silicon Inorganic materials 0.000 claims abstract description 24
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 24
- 239000010703 silicon Substances 0.000 claims abstract description 23
- 229910052751 metal Inorganic materials 0.000 claims abstract description 15
- 239000002184 metal Substances 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 8
- 239000011812 mixed powder Substances 0.000 claims description 34
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 19
- 239000001301 oxygen Substances 0.000 claims description 19
- 238000009792 diffusion process Methods 0.000 claims description 8
- 229930195733 hydrocarbon Natural products 0.000 claims description 8
- 150000002430 hydrocarbons Chemical class 0.000 claims description 8
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 238000000859 sublimation Methods 0.000 claims description 4
- 230000008022 sublimation Effects 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 27
- 239000000203 mixture Substances 0.000 abstract description 8
- 229910004298 SiO 2 Inorganic materials 0.000 description 38
- 238000007254 oxidation reaction Methods 0.000 description 21
- 235000012239 silicon dioxide Nutrition 0.000 description 18
- 229910052681 coesite Inorganic materials 0.000 description 16
- 229910052906 cristobalite Inorganic materials 0.000 description 16
- 229910052682 stishovite Inorganic materials 0.000 description 16
- 229910052905 tridymite Inorganic materials 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 239000002360 explosive Substances 0.000 description 10
- 239000007773 negative electrode material Substances 0.000 description 9
- 229910001873 dinitrogen Inorganic materials 0.000 description 8
- 239000003949 liquefied natural gas Substances 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 230000003647 oxidation Effects 0.000 description 7
- 239000007790 solid phase Substances 0.000 description 7
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 5
- 239000012159 carrier gas Substances 0.000 description 5
- 229910001416 lithium ion Inorganic materials 0.000 description 5
- 229910052786 argon Inorganic materials 0.000 description 3
- 238000007323 disproportionation reaction Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910018557 Si O Inorganic materials 0.000 description 2
- 238000002441 X-ray diffraction Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
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- 239000007791 liquid phase Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 239000006223 plastic coating Substances 0.000 description 2
- 238000001144 powder X-ray diffraction data Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000220317 Rosa Species 0.000 description 1
- 229910004205 SiNX Inorganic materials 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
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- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
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- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
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- 230000020169 heat generation Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D7/00—Sublimation
- B01D7/02—Crystallisation directly from the vapour phase
Definitions
- the present invention relates to a method for producing silicon monoxide.
- SiO silicon monoxide
- metal silicon powder hereinafter also referred to as “Si” or “Si powder”
- silica powder hereinafter referred to as , SiO 2 or SiO 2 powder
- the SiO gas is vapor-deposited on a vapor deposition plate, cooled, and solidified into bulk SiO.
- SiO gas In order to generate SiO gas, it is necessary to increase the number of contact points between Si/SiO 2 powders, and the fine powders are mixed and granulated or compacted in some way to increase the contact points to promote the reaction.
- a higher reaction temperature is desirable, but if the reaction temperature is too high, the metallic silicon Si will melt, making it difficult to retain the liquid.
- it is effective to press the powders strongly, but there is a limit because both Si and SiO 2 are ceramics and do not deform.
- Non-Patent Document 1 SiO 2 +C ⁇ SiO + CO (2) SiO+C ⁇ Si+CO (3) SiO 2 +2C ⁇ Si+2CO It is desirable to stop at the above step (1) of C reduction of SiO 2 and extract only SiO.
- the processes (1) to (3) occur continuously in the reducing furnace, and the generated SiO gas undergoes the reaction (2) immediately in the molten metal to generate molten Si.
- Patent Documents 8 and 9 methods for producing fine SiO 2 or composite oxides of fine SiO 2 + another oxide by explosive combustion of Si and O 2 are disclosed in the following prior art documents (Patent Documents 8 and 9).
- Patent Document 9 it is devised that "metallic silicon powder is supplied into an oxygen-containing gas stream and burned to form silicon dioxide powder having an average particle size of 0.01 to 10 ⁇ m", and fine SiO 2 powder. is already known.
- Patent Documents 10 and 11 SiO generation by an explosive combustion method and SiN x generation via SiO are also disclosed (Patent Documents 10 and 11), but the conditions are not specifically described, and the details of the technology are unknown. is. Moreover, in Patent Document 10, SiO is generated in a plasma jet, which is completely different from the generation reaction in a flame containing O 2 . In Patent Document 11, SiO generation by oxidation in flame and SiNx generation by flame nitridation in the next step are continuously performed, and it is not known whether only SiO can be extracted by flame oxidation.
- the present invention has been made in view of the above problems, and an object of the present invention is to provide a highly productive method for producing silicon monoxide by controlling the O 2 concentration during the explosive combustion reaction.
- the present invention provides a method for producing silicon monoxide (SiO), which comprises a method of producing silicon monoxide ( SiO), comprising: An operation A of supplying the mixed powder to a combustion device using a first mixed gas containing oxygen gas and an inert gas as a carrier; 2, forming a flame, and reacting the silicon (Si) component derived from the metal silicon (Si) powder with the oxygen gas in the flame to obtain a product.
- the operation B when the operation B is performed, the operation A is also performed at the same time, and the amount of the metal silicon (Si) powder supplied to the combustion device, the oxygen gas contained in the first mixed gas, and the second mixed gas
- the reaction of the silicon (Si) component and the oxygen gas is performed under conditions where silicon monoxide (SiO) powder is generated.
- a method for producing (SiO) is provided.
- SiO powder is efficiently produced by oxidation reaction of Si powder or a mixed powder of Si powder and SiO2 powder in an air stream, which is very productive compared to the conventional solid-phase contact reaction method. be able to generate.
- the combustion device contains oxygen gas and an inert gas for controlling oxygen diffusion into the metallic silicon (Si) powder or mixed powder of metallic silicon (Si) powder and silica (SiO 2 ) powder.
- An operation C of supplying a third mixed gas or an inert gas may be further provided, and when the operation B is performed, the operation C may also be performed at the same time.
- the gas for controlling oxygen diffusion into Si powder or mixed powder of Si powder and SiO2 powder can control the generation of SiO powder with higher precision.
- the combustible gas contained in the second mixed gas can contain hydrocarbon.
- the combustible gas contained in the second mixed gas may contain hydrogen.
- the SiO contained in the product can be extracted by sublimation by heating the product at a temperature of 1100°C or higher and 1500°C or lower.
- SiO 2 silicon dioxide
- SiO powder is efficiently produced by an oxidation reaction in an airflow of Si powder or a mixed powder of Si powder and SiO2 powder, which is very productive compared to the conventional solid-phase contact reaction method. be able to generate.
- SiO produced by the method for producing SiO of the present invention can be used as a negative electrode material for lithium ion secondary batteries, in addition to glass and plastic coating applications.
- such a negative electrode material can be widely used as a high-capacity negative electrode material for mobile devices such as smartphones and smart watches, and batteries for electric vehicles.
- FIG. 1 is a schematic cross-sectional view showing an example of a combustion apparatus that can be used in the method for producing SiO of the present invention
- FIG. 4 is a schematic cross-sectional view showing another example of a combustion apparatus that can be used in the SiO production method of the present invention.
- FIG. 4 is a schematic cross-sectional view showing still another example of a combustion apparatus that can be used in the method for producing SiO of the present invention.
- 1 is a binary phase diagram of Si—O; FIG.
- the conventional solid-phase contact method has limitations in the efficient production of SiO.
- SiO is very important as a negative electrode material for improving the performance of lithium ion secondary batteries in the future, and its application is expanding. Therefore, an efficient manufacturing method and SiO production maintaining a low disproportionation state are desired.
- the present invention relates to a method for producing silicon monoxide (SiO), wherein metallic silicon (Si) powder or a mixed powder of metallic silicon (Si) powder and silica powder (SiO 2 ), which is a raw material, is mixed with oxygen gas.
- Operation A of supplying a first mixed gas containing an active gas as a carrier to a combustion device, and supplying a second mixed gas containing a combustible gas, an oxygen gas and an inert gas to the combustion device.
- the silicon (Si) A method for producing silicon monoxide (SiO), characterized in that a reaction between a component and oxygen gas is carried out under conditions that generate silicon monoxide (SiO) powder.
- the combustion device contains oxygen gas and an inert gas for controlling diffusion of oxygen into the metallic silicon (Si) powder or mixed powder of metallic silicon (Si) powder and silica (SiO 2 ) powder. 3, or the operation C of supplying the inert gas, and the operation C may be performed at the same time as the operation B is performed.
- FIG. 4 shows a binary phase diagram of Si—O.
- the temperature In order to turn SiO2 into a gas phase, it is necessary to raise the temperature to over 2,860°C. This is the lower temperature limit for SiO gas phase formation. Therefore, it is sufficient if the temperature can be raised above this temperature in an oxidizing atmosphere.
- the raw material is a mixed powder of Si powder and SiO 2 powder
- the contact sublimation reaction between solid phases originally occurs sufficiently at 1,300° C. or higher.
- the vapor pressures of Si and SiO2 In the temperature field raised to 1,860°C or higher, as in the present invention, the vapor pressures of Si and SiO2 are different, but reactions occur sufficiently whether they are liquid droplets or vapor gas, and SiO is formed. be done.
- FIG. 1 shows an example of a combustion device (combustion reaction device) that is important for realizing the SiO production method of the present invention.
- the combustion reaction apparatus is not limited to the apparatus shown in FIG. 1, and the method for producing SiO of the present invention can be carried out with any apparatus capable of controlling flame and combustion oxidation.
- a SiO manufacturing apparatus (combustion apparatus) 100 has a combustion vessel 10 .
- the combustion vessel 10 is supplied with a supply means 11 for Si powder or a mixed powder of Si powder and SiO 2 powder (illustrated as means for supplying Si powder) and a first mixed gas containing oxygen gas and inert gas.
- a first gas supply means 12 is connected through a burner 13 .
- the first gas supply means 12 shows a case where nitrogen gas (N 2 gas) is added to air to form a first mixed gas.
- the flow rate of the inert gas is adjusted by the added nitrogen gas together with the nitrogen and argon contained in the air.
- the raw material Si powder or Si powder and SiO 2 powder mixed powder uses the first mixed gas containing oxygen gas and inert gas as a carrier, and the combustion device 100 (the combustion chamber of the combustion device 100 10).
- the combustion device 100 further includes second gas supply means for supplying a second mixed gas containing a combustible gas, an oxygen gas, and an inert gas to the combustion device 100 (inside the combustion vessel 10 of the combustion device 100).
- second gas supply means 14 supplies LPG, air, and additional nitrogen gas.
- the combustion device 100 further includes a third mixed gas containing oxygen gas and an inert gas for controlling oxygen diffusion into the Si powder, or , a third gas supply means for supplying an inert gas.
- FIG. 1 shows a case where air and additional nitrogen gas are mixed and supplied as the third gas supply means 15 .
- the combustion apparatus 100 may further include protection gas supply means 16 and 17 for supplying protection gas for purposes such as reducing radiant heat to the furnace wall.
- protection gas supply means 16 and 17 for supplying protection gas for purposes such as reducing radiant heat to the furnace wall.
- FIG. 1 shows a case where air and additional nitrogen gas are mixed and supplied as third gas supply means 16 and 17 .
- the combustion device 100 further comprises a collecting chamber 23 for collecting the generated SiO powder 24 at its lower portion.
- SiO can be produced using such a combustion apparatus 100 . That is, from the upper center of the combustion apparatus 100, the Si powder or the mixed powder of Si powder and SiO 2 powder is supplied to the first mixed gas by the Si powder or the mixed powder of Si powder and SiO 2 powder by means of supplying means 11 and the first gas supplying means 12. (In the case of FIG. 1, air and additional nitrogen gas) are supplied together with a carrier gas stream (operation A). At this time, the Si powder or the mixed powder of the Si powder and the SiO 2 powder can be, for example, about #200 mesh.
- a second mixed gas in the case of the example of FIG. 1, a combustible gas consisting of LPG, air, and additional nitrogen gas is supplied from the concentric periphery.
- the tip of the burner 13 is ignited to form a flame 21 .
- the Si powder is oxidized in the flame 21 or the mixed powder of the Si powder and the SiO 2 powder is reacted while supplementing the insufficient amount with oxygen gas to oxidize it, and it is rapidly cooled and solidified as SiO gas in the lower part of the device to generate SiO powder ( Operation B).
- the ratio of the Si powder and the SiO 2 powder mixed powder is preferably Si-rich, and is preferably about 1.5 ⁇ Si/SiO 2 ⁇ 3.
- a third mixed gas containing oxygen gas and inert gas in the case of FIG.
- the second mixed gas containing combustible gas, oxygen gas (combustion-supporting O2 gas), and inert gas is supplied to the combustion device to form a flame. It is the main heat source for oxidation of powder or mixed powder of Si powder and SiO2 powder. Then, Si powder (Si fine powder) or Si powder and SiO 2 powder mixed powder as a raw material is combusted with a first mixed gas containing oxygen gas (combustion-supporting O 2 gas) and inert gas as a carrier.
- the operation A to supply to the device exists in the same combustion device, and the temperature is raised to the SiO gas temperature range described above while adding the heat of oxidation of the Si powder or the mixed powder of Si powder and SiO 2 powder and oxygen gas. SiO is produced.
- a mixed gas of an inert gas (first mixed gas) is used as a carrier in addition to the combustion-supporting O2 gas in operation A is to control the oxidation reaction of the Si powder or the mixed powder of the Si powder and the SiO2 powder.
- the carrier gas is only combustion-supporting O 2 gas, an explosive oxidation reaction may occur instantaneously to produce SiO 2 . Therefore, a mixed gas of a combustion-supporting O 2 gas and an inert gas is used to dilute the O 2 concentration to control the oxidation exothermic reaction rate and facilitate the generation of SiO. In order to stop the reaction with SiO without reaching SiO 2 formation, it is necessary not to exceed the explosion limit oxygen concentration of 10%.
- the first mixed gas a mixed gas of O 2 and N 2 , a mixed gas of O 2 and Ar, or the like whose amount ratio is controlled is desirable.
- operation B is an operation of supplying a mixed gas (second mixed gas) of combustible gas, oxygen gas (combustible O2 gas) and inert gas to form a flame.
- This operation is the main heat supply step for converting Si or mixed powder of Si and SiO2 into SiO.
- a mixed gas of combustible gas and oxygen gas is used. Adjust the amount of heat with (second mixed gas).
- an inert gas is also added to regulate and control the SiO production rate.
- the inert gas here may be nitrogen, argon, or the like contained in the air.
- the combustible gas may be a hydrocarbon gas such as CH 4 or LPG (liquefied natural gas), and of course the hydrocarbon gas is not limited to these. Hydrocarbons such as methane, ethane, propane, acetylene, and propylene are preferable because sufficient combustion heat generation can be obtained, but they are not limited to these.
- the combustible gas may be hydrogen ( hereinafter referred to as H2) or a mixed gas of H2 and hydrocarbons. The ratio and the like may be determined so that the shape of the flame, such as the amount of heat generated in the flame and the length of the flame, can be adapted to the generation of SiO.
- Operation B is an essential step for forming a flame and reacting Si powder or Si/ SiO2 mixed powder with O2 gas in the flame to generate SiO.
- the size of the flame is increased as long as possible, and the Si component is oxidized as slowly as possible in the flame to form SiO while controlling it.
- Oxidation reaction control particularly depends on the amount of Si powder or Si and SiO 2 mixed powder supplied to the combustion device and the amount of oxygen gas (oxygen gas contained in the first mixed gas and oxygen contained in the second mixed gas by adjusting the ratio to the total amount of gas). Furthermore, it is possible to control the oxidation reaction by optimizing the mixing ratio and type of combustible gas ( hydrocarbon gas, H2, etc.), and the mixing ratio of combustible gas, oxygen gas (combustion-supporting gas), and inert gas. preferable. In other words, since the proper amount of O 2 in the flame changes depending on the Si supply amount, combustible gas species, flow rate, etc., these generation conditions can be adjusted experimentally.
- the combustion apparatus is equipped with a third mixed gas containing oxygen gas and an inert gas for controlling oxygen diffusion into the Si powder or the mixed powder of Si and SiO2 .
- it may further comprise an operation C of supplying an inert gas.
- the amount of Si powder or mixed powder of Si and SiO 2 to be supplied is small, the amount of O 2 required may naturally be small. In that case, if the amount of combustion-supporting O2 gas in operation B is reduced, the flame cannot be optimized. Therefore, the mixed gas in operation B maintains the flame within the adjustment range, and in operation C, the O 2 /inert gas ratio is adjusted to the O 2 less side (the side with less O 2 ) is supplied. Conversely, when the amount of Si powder or mixed powder of Si and SiO 2 supplied is large, the O 2 /inert gas ratio is adjusted to the O 2 -rich side (the O 2 -rich side) in operation C.
- the supply of the protect gas from the protect gas supply means 16 and 17 supplies a third mixed gas containing oxygen gas and an inert gas or an inert gas for controlling oxygen diffusion to the Si powder. It is also part of the operation C of doing.
- SiO silicon ion battery
- SiO produced by the production method of the present invention can be used as a negative electrode material for lithium ion secondary batteries in addition to glass and plastic coating applications. Furthermore, it can be widely used as a high-capacity negative electrode material for mobile devices such as smartphones and smart watches, and batteries for electric vehicles.
- SiO can be produced with good productivity by the above - mentioned method. was obtained in some cases.
- the SiO contained in the product can be extracted by sublimation by heating the product at a temperature of 1100° C. or higher and 1500° C. or lower. Since the temperature at which Si and SiO 2 vaporize is much higher than that of SiO, only the SiO component can be sublimated and extracted by such a method.
- Example 1 Using the combustion apparatus (combustion reaction apparatus) 100 shown in FIG. 1, SiO was produced according to the production method of the present invention.
- the combustible gas used in Operation B was LPG. Air was used as the O 2 gas and the inert gas, and the third mixed gas used in operation C was air (that is, a mixed gas containing oxygen gas and nitrogen and argon as inert gases).
- Si powder supply means 11 2.5 kg/hr of Si powder was supplied from the Si powder supply means 11 .
- This Si powder was supplied by supplying 1.5 m 3 /hr of a carrier gas (O 2 concentration of 10 vol%), which is a mixture of air and additional N 2 gas, from the first gas supply means 12 (operation A). Also, the burner 13 was ignited.
- a carrier gas O 2 concentration of 10 vol%, which is a mixture of air and additional N 2 gas
- SiO powder was generated while controlling the amount of O 2 in the combustion flame 21 .
- Example 2 The raw material to be supplied was a mixed powder of Si and SiO 2 (ratio 2:1), and was supplied from the supply means 11 at 2.5 kg/hr.
- the powder was supplied by supplying 1.5 m 3 /hr of a carrier gas (target O 2 concentration of 7 vol%), which is a mixture of air and additional N 2 gas, from the first gas supply means 12 (operation A ).
- SiO powder was produced while controlling the amount of O 2 in the combustion flame 21 by the same operations A, B, and C as in Example 1 except for this. It was confirmed from the powder XRD pattern of the SiO powder of this example that it was amorphous.
- Example 3 SiO was manufactured using the SiO manufacturing apparatus 200 shown in FIG.
- the configuration of the SiO manufacturing apparatus 200 of FIG. 2 is basically the same as that of FIG. 2) is different.
- Other configurations denoted by the same reference numerals are the same as in FIG.
- H 2 gas was supplied from the hydrogen gas supply means 34a instead of the hydrocarbon gas (LPG), which is the combustible gas in Example 1, and was used as the main heat source.
- LPG hydrocarbon gas
- the flame is mainly controlled in operation B, it is possible to introduce air and additional oxygen gas ( O2 gas) from the air and oxygen gas supply means 34b while mixing with the above H2 ( however, in this embodiment By adjusting, the amount of air introduced was set to zero as described later), and the amount of oxygen in the flame was adjusted.
- O2 gas additional oxygen gas
- the protect gas is air+ N2 , and the amount of oxygen in the tank (inside the combustion vessel 10) is adjusted and controlled.
- the amount of Si powder supplied from the Si powder supply means 11 was set to 2.5 kg/hr, which is the same as in Example 1, and the amount of accompanying carrier gas was set to be the same as in Example 1.
- 8 Nm 3 /hr of H 2 gas is introduced from the hydrogen gas supply means 34a, and 5 Nm 3 /hr of O 2 gas (0% air in this embodiment) is supplied from the air and oxygen gas supply means 34b to 100 m/hr from the nozzle.
- a H 2 /O 2 hydrolysis flame was formed, introduced from a coaxial burner with an initial velocity of up to sec.
- SiO was manufactured using the SiO manufacturing apparatus 300 shown in FIG.
- the size of the flame 21 formed in the operation B is increased, and the flame reaction of the multi-burner structure is performed so that the SiO generation reaction in the flame can be carried out in a mild and controlled state for a long time. device.
- the basic structure of the combustion reactor of this embodiment is the same as that of Embodiments 1 and 2, but the second gas supply means (burner device) for operation B is placed on the top of the furnace, and the combustion vessel 10 at the bottom is also equipped with A plurality of second gas supply means (burner devices) such as 44a, 44b, 44c, and 44d were provided in order, the SiO reaction generation zone was lengthened, and the reaction was carried out while controlling the amount of oxygen.
- the lower burner arrangement of the present invention is not limited to the arrangement shown in FIG.
- the conditions for operation A are the same as in Example 1.2.
- the gas conditions for operation B ranged from 0.5 to 1.0 Nm 3 /hr of LPG and from 12 to 24 Nm 3 /hr of the second mixed gas (air), and were selected to be optimal for SiO production.
- XRD analysis of the produced SiO powder confirmed that it was amorphous with only broad reflections and no Si peak was observed as in Examples 1 and 2.
- Analysis of the reaction product revealed that SiO was 95% or more, and the balance was unreacted Si powder and SiO 2 powder.
- the present invention is not limited to the above embodiments.
- the above-described embodiment is an example, and any device having substantially the same configuration as the technical idea described in the claims of the present invention and exhibiting the same effect is the present invention. included in the technical scope of
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Abstract
Description
(1) SiO2+C → SiO+CO
(2) SiO+C → Si+CO
(3) SiO2+2C → Si+2CO
SiO2のC還元の上記(1)過程で止めて、SiOのみを取り出せると望ましい。しかし、還元炉の中で(1)~(3)過程は連続的に起きており、生成したSiOガスは溶湯中で直ちに(2)の反応が起きて、溶融Siが生成する。(1)過程で止めてSiOのみを取り出すことは難しい。(1)過程の還元炉中に高温耐性のあるパイプを挿入などして、SiOガスを取り出しすることも原理的には考えられるが、実際に実行された例はない。
操作Aで支燃性O2ガス以外に不活性ガスの混合ガス(第1の混合ガス)をキャリアとするのは、Si粉末またはSi粉末とSiO2粉末混合粉の酸化反応を制御するためである。キャリアガスが支燃性のO2ガスのみであると、瞬時に爆発的酸化反応が起きて、SiO2が生成してしまう可能性がある。そのため支燃性のO2ガスと不活性ガスの混合ガスとして、O2濃度を薄めて酸化発熱反応速度を制御し、SiOを生成し易くするものである。SiO2生成まで至らずSiOで反応を停止させるには、爆発限界酸素濃度10%を超えないようにする必要がある。該第1の混合ガスとして、O2とN2の混合ガス、O2とArの混合ガスなどの量比を制御したものが望ましい。
上記のように、操作Bは、可燃性ガスと酸素ガス(支燃性O2ガス)と不活性ガスの混合ガス(第2の混合ガス)を供給し、火焔を形成する操作である。この操作がSiまたはSiとSiO2混合粉をSiOとするための主たる熱供給工程となる。操作Aで混合ガス(第1の混合ガス)を空気とした場合、SiO生成のためのO2が不足するため、操作Bでは可燃性ガスと酸素ガス(支燃性O2ガス)の混合ガス(第2の混合ガス)で熱量を調整する。さらに、操作Aと同じように、操作Bでは、SiO生成速度を調整制御するため、不活性ガスも加える。ここでの不活性ガスは空気に含まれる窒素、アルゴン等でもよい。
上記のように、供給されるSi粉末またはSiとSiO2混合粉の量に応じて、操作Bにおける第2の混合ガスのガス比率は最適化する必要があるが、火焔の最適化と両立しない場合もある。言い換えれば、火焔最適化とは火焔を出来るだけ長くすることである。本発明ではSi粉末またはSiとSiO2混合粉を火焔内に落下させながら、制御酸化してSiOを生成するが、火焔長さや温度分布と酸素量制御が両立しない場合がある。その場合、Si粉末またはSiとSiO2混合粉への酸素拡散を制御するO2/不活性ガスあるいは不活性ガスを供給する操作Cにより、操作Bにおける酸化速度を制御することができるようになる。具体的には、本発明のSiOの製造方法において、燃焼装置に、Si粉末またはSiとSiO2混合粉への酸素拡散を制御するための、酸素ガスと不活性ガスを含む第3の混合ガス、又は、不活性ガスを供給する操作Cをさらに有するものとすることができる。Si粉末またはSiとSiO2混合粉の供給量が少ない時は、当然必要とされるO2量は少なくてよい。その場合、操作Bにおける支燃性O2ガス量を少なくしてしまうと、火焔を最適化できなくなる。そこで操作Bの混合ガスは調整範囲で火焔を維持し、操作CにおいてO2/不活性ガス比率をO2レス側(O2が少ない側)に調整したものを供給する。Si粉末またはSiとSiO2混合粉の供給量が多い時は逆で、操作CにおいてO2/不活性ガス比率をO2リッチ側(O2が多い側)にして調整する。
図1に示した燃焼装置(燃焼反応装置)100を用いて、本発明の製造方法に従って、SiOを製造した。操作Bに用いる可燃性ガスはLPGとした。O2ガスと不活性ガスを空気とし、操作Cに用いる第3の混合ガスは、空気(すなわち、酸素ガスを含み、不活性ガスとして窒素及びアルゴンを含む混合ガス)とした。
供給する原料がSiとSiO2混合粉(比率2:1)で、供給手段11より、2.5kg/hrを供給した。該粉末は、空気と追加N2ガスを混合したキャリアガス(O2濃度7Vol%目途)1.5m3/hrを第1のガス供給手段12から供給してこれに乗せて供給した(操作A)。これ以外は実施例1と同じ操作A、B、Cにより、燃焼火焔21内でO2量を制御しながら、SiOの粉末を生成させた。本実施例のSiO粉末による粉末XRD図形からアモルファス状であることが確認できた。
図2に示したSiOの製造装置200を用いてSiOを製造した。図2のSiOの製造装置200の構成は図1と基本的に同様であるが、第2のガス供給手段34から、H2ガス及び空気と追加酸素ガス(O2ガス)の混合ガス(第2の混合ガス)を供給することが異なる。その他の同一の符号を付した構成は図1と同様である。操作Bでは、実施例1の可燃性ガスである炭化水素ガス(LPG)の代わりに水素ガス供給手段34aからH2ガスを供給し主たる発熱源とした。また、操作Bで主に火焔を制御するが、空気及び酸素ガス供給手段34bから空気と追加酸素ガス(O2ガス)を、上記のH2と混合しながら導入可能(ただし、この実施例では調整により、後述のように空気の導入量をゼロとした。)なものとし、火焔中の酸素量を調整した。
図3に示したSiOの製造装置300を用いてSiOを製造した。このSiOの製造装置300では、操作Bで形成する火焔21のサイズを長くして、火焔内でのSiO生成反応が永くマイルドにかつ制御された状態で行われるように、マルチバーナー構造の火焔反応装置とした。
図1に示した実施例1と実施例2の装置における操作Cの第3のガス供給手段15から100%O2ガスを供給した。火焔21内で酸素リッチな状態になり、火焔温度も上昇して、反応がSiOで止まらない比率が増えた。生成物をXRD解析したところ、ほとんどがSiO2粒子であった。
Claims (5)
- 一酸化珪素を製造する方法であって、
原料となる金属珪素粉末または金属珪素粉末とシリカ粉末の混合粉を、酸素ガスと不活性ガスとを含む第1の混合ガスをキャリアとして、燃焼装置に供給する操作Aと、
前記燃焼装置に、可燃性ガスと酸素ガスと不活性ガスとを含む第2の混合ガスを供給して火焔を形成し、該火焔中で前記金属珪素粉末由来の珪素成分と前記酸素ガスを反応させることにより生成物を得る操作Bと
を有し、
前記操作Bを行う際に操作Aも同時に行われ、
前記燃焼装置に供給する前記金属珪素粉末の量と、前記第1の混合ガスに含まれる酸素ガス及び前記第2の混合ガスに含まれる酸素ガスの合計量との比を調整することにより、前記珪素成分と酸素ガスの反応を一酸化珪素粉末が生成する条件で行うことを特徴とする一酸化珪素の製造方法。 - 前記燃焼装置に、前記金属珪素粉末または金属珪素粉末とシリカ粉末の混合粉への酸素拡散を制御するための、酸素ガスと不活性ガスを含む第3の混合ガス、又は、不活性ガスを供給する操作Cをさらに有し、
前記操作Bを行う際に操作Cも同時に行われることを特徴とする請求項1に記載の一酸化珪素の製造方法。 - 前記第2の混合ガスに含まれる可燃性ガスを、炭化水素を含むものとすることを特徴とする請求項1又は請求項2に記載の一酸化珪素の製造方法。
- 前記第2の混合ガスに含まれる可燃性ガスを、水素を含むものとすることを特徴とする請求項1から請求項3のいずれか1項に記載の一酸化珪素の製造方法。
- 前記生成物を、1100℃以上1500℃以下の温度で加熱することにより、前記生成物に含まれる一酸化珪素を昇華抽出することを特徴とする請求項1から請求項4のいずれか1項に記載の一酸化珪素の製造方法。
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