CN214681632U - Material synthesis system - Google Patents
Material synthesis system Download PDFInfo
- Publication number
- CN214681632U CN214681632U CN202023120597.3U CN202023120597U CN214681632U CN 214681632 U CN214681632 U CN 214681632U CN 202023120597 U CN202023120597 U CN 202023120597U CN 214681632 U CN214681632 U CN 214681632U
- Authority
- CN
- China
- Prior art keywords
- outlet
- reaction raw
- vaporizer
- bed reactor
- raw material
- 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
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The application discloses a material synthesis system. This material synthesis system includes: a vaporizer and a fluidized bed reactor, wherein: the vaporizer is provided with a reaction raw material inlet, a reaction raw material outlet and a drain outlet for discharging easily blocked substances in the reaction raw materials; and a reaction raw material inlet in the fluidized bed reactor is connected with a reaction raw material outlet in the vaporizer. Because the fluidized bed reactor is connected with the vaporizer and the vaporizer is provided with the drain outlet for discharging the easily blocked substances in the reaction raw materials, the easily blocked substances in the reaction raw materials can be discharged from the drain outlet through the vaporizer, thereby avoiding the excessive easily blocked substances from entering the fluidized bed reactor and reducing the possibility that the distribution plate is blocked by the easily blocked substances.
Description
Technical Field
The application relates to the field of chemical synthesis, in particular to a material synthesis system.
Background
In the catalytic synthesis process, it is usually necessary to add a distribution plate in the fluidized bed reactor to increase the contact between different reactants. For example, in the catalytic synthesis of methylchlorosilane, a distribution plate is required to be added in the fluidized bed reactor to increase the contact between the two reactants, i.e. methyl chloride and silicon powder. Thus, the distribution plate has a significant effect on whether the catalytic synthesis process can proceed smoothly, and it is desirable to avoid the distribution plate from being clogged by certain components of the reactants during the catalytic synthesis process.
SUMMERY OF THE UTILITY MODEL
The embodiment of the application provides a material synthesis system.
The embodiment of the application provides a material synthesis system, includes: a vaporizer and a fluidized bed reactor, wherein: the vaporizer is provided with a reaction raw material inlet, a reaction raw material outlet and a drain outlet for discharging easily blocked substances in the reaction raw materials; and the number of the first and second groups,
and a reaction raw material inlet in the fluidized bed reactor is connected with a reaction raw material outlet in the vaporizer.
Preferably, the sewage draining outlet is arranged at the bottom of the vaporizer; or the like, or, alternatively,
the sewage draining outlet is arranged on the side wall of the lower end of the vaporizer.
Preferably, the material synthesis system further comprises a superheater, wherein:
the superheater is arranged in a connecting pipeline between a reaction raw material inlet of the fluidized bed reactor and a reaction raw material outlet of the vaporizer.
Preferably, the material synthesis system further comprises a cyclone separator and a washing tower;
a synthetic product outlet of the fluidized bed reactor is connected with a material inlet of the cyclone separator; and the gas phase outlet of the cyclone separator is connected with the material inlet of the washing tower.
Preferably, the material synthesis system further comprises an evaporator; the washing tower also comprises a liquid-phase material outlet and a reclaimed material inlet;
a liquid-phase material outlet in the washing tower is connected with a material inlet of the evaporator; and the number of the first and second groups,
and a recycled material inlet in the washing tower is connected with a gas-phase material outlet of the evaporator.
Preferably, the evaporator further comprises a second material inlet connected with the sewage draining outlet.
Preferably, a flow meter and a regulating valve are arranged in a connecting pipeline between the sewage draining outlet and the second material inlet.
Preferably, a sampling point is arranged in a connecting pipeline between the sewage draining outlet and the second material inlet; and the sampling point is connected with a sampling pipeline.
Preferably, the solid phase outlet of the cyclone separator is connected with a recovery device; and the number of the first and second groups,
and a gas-phase material outlet of the washing tower is connected with a synthetic product conveying pipeline.
Preferably, the synthesis product outlet in the fluidized bed reactor is arranged at the upper end of the fluidized bed reactor.
The embodiment of the application adopts at least one technical scheme which can achieve the following beneficial effects:
adopt this material synthesis system that this application embodiment provided, it includes vaporizer and fluidized bed reactor, wherein: the vaporizer is provided with a reaction raw material inlet, a reaction raw material outlet and a drain outlet for discharging easily blocked substances in the reaction raw materials; and a reaction raw material inlet in the fluidized bed reactor is connected with a reaction raw material outlet in the vaporizer. Because the fluidized bed reactor is connected with the vaporizer and the vaporizer is provided with the drain outlet for discharging the easily blocked substances in the reaction raw materials, the easily blocked substances in the reaction raw materials can be discharged from the drain outlet through the vaporizer, thereby avoiding the excessive easily blocked substances from entering the fluidized bed reactor and reducing the possibility that the distribution plate is blocked by the easily blocked substances.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
fig. 1 is a schematic structural diagram of a material synthesis system provided in an embodiment of the present application.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more apparent, the technical solutions of the present application will be described in detail and completely with reference to the following specific embodiments of the present application and the accompanying drawings. It should be apparent that the described embodiments are only some of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
The technical solutions provided by the embodiments of the present application are described in detail below with reference to the accompanying drawings.
As mentioned above, it is often necessary to add distribution plates in the fluidized bed reactor during the catalytic synthesis process to increase the contact between the different reactants. For example, when methyl chlorosilane is synthesized in a fluidized bed reactor, a distribution plate arranged in the fluidized bed reactor is needed to increase the contact between methyl chloride and silicon powder. Therefore, it is desirable to avoid clogging of the distribution plate by certain components in the reactants.
Based on this, the present application provides a material synthesis system, which can reduce the possibility that a distribution plate is blocked by easily-blocking substances in reactants, thereby solving the problems in the prior art. As shown in fig. 1, a detailed structural diagram of the material synthesizing system 100 is shown, and the material synthesizing system 100 includes: a vaporizer 1 and a fluidized bed reactor 2.
The vaporizer 1 is provided with a reaction raw material inlet 11, a reaction raw material outlet 12, and a drain outlet 13, wherein the reaction raw material inlet 11 is used to introduce a reaction raw material, which may be a liquid reaction raw material in general, into the vaporizer 1, and then the reaction raw material is heated and vaporized by the vaporizer 1. The reaction raw material outlet 12 can lead out the reaction raw material vaporized in the vaporizer 1.
In practical applications, the reaction raw material for material synthesis may contain other substances due to insufficient purity, which tend to block the distribution plate in the fluidized bed reactor 2, and the boiling point of the easily-blocked substances is generally higher than that of the reactants, i.e., the easily-blocked substances are more difficult to evaporate into a gaseous state, according to the characteristics of the substances. Therefore, in the vaporizer 1, the reaction raw material can be vaporized by heating, so that the reaction raw material is discharged from the reaction raw material outlet 12 of the vaporizer 1, and the easily-clogged substance is discharged through the drain outlet 13, thereby preventing excessive easily-clogged substance from entering the fluidized bed reactor 2, and reducing the possibility that the distribution plate is clogged by the easily-clogged substance. In the case where the reaction raw material is heated and vaporized in the vaporizer 1, the temperature in the vaporizer 1 may be set to about the boiling point of the reaction raw material or slightly lower than the boiling point of the reaction raw material, in consideration of the boiling points of the reaction raw material and the easily-clogging substance.
For example, in the process of synthesizing methylchlorosilane, chloromethane is introduced into the vaporizer 1 as the reaction raw material, and the temperature in the vaporizer 1 may be set to about 23.7 degrees celsius (boiling point temperature of monochloromethane) or slightly lower than 23.7 degrees celsius, so that monochloromethane is evaporated into a gaseous state and is discharged from the reaction raw material outlet 12; while for other components, such as carbon tetrachloride and the like, which are present in the vaporizer 1 mainly in liquid form due to their relatively high boiling point, they can be discharged from the blow-off 13.
In addition, as for the specific positions where the reaction raw material inlet 11, the reaction raw material outlet 12, and the drain outlet 13 are provided in the vaporizer 1, the reaction raw material outlet 12 may be provided at the upper end of the vaporizer 1 so that the reaction raw material after vaporization is easily led out, and both the reaction raw material inlet 11 and the drain outlet 13 may be provided at the lower end of the vaporizer 1.
For example, the reaction raw material outlet 12 is provided on the top of the vaporizer 1, or on the side wall of the upper end; the sewage draining outlet 13 can also be arranged at the bottom of the vaporizer 1 or on the side wall at the lower end, so that the discharge of substances is easy to block; the reaction material inlet 11 may be provided in the bottom of the vaporizer 1 or in the lower side wall thereof, since the liquid reaction material is usually introduced. Wherein, for the upper end and the lower end of the vaporizer 1, the upper end can generally refer to the position where the distance from the top of the vaporizer 1 is 0-30% of the total height of the vaporizer 1, the lower end can refer to the position where the distance from the top of the vaporizer 1 is 70-100% of the total height of the vaporizer 1, and subsequently, for the upper end and the lower end of the fluidized bed reactor 2, the upper end and the lower end of the cyclone 4 or the upper end and the lower end of other equipment, the upper end can also be understood as the position where the distance from the top of the corresponding equipment is 0-30% of the total height of the equipment, and the lower end can be understood as the position where the distance from the top of the corresponding equipment is 70-100% of the total height of the equipment.
The fluidized bed reactor 2 in the material synthesizing system 100 is mainly used for performing chemical reactions between various reaction raw materials so as to synthesize required materials. The fluidized-bed reactor 2 includes a reaction raw material inlet 21, and the reaction raw material inlet 21 is connected to the reaction raw material outlet 12 of the vaporizer 1 to introduce the reaction raw material into the fluidized-bed reactor 2.
The reaction raw material inlet 21 may be generally disposed at the bottom of the fluidized-bed reactor 2, and the gaseous reaction raw material flows upward after entering the fluidized-bed reactor 2 through the reaction raw material inlet 21 and is sufficiently contacted with other reaction raw materials (e.g., silicon powder) at the distribution plate a.
The material synthesis system 100 may further include a superheater 3, and the superheater 3 is disposed in a connection pipe between the reaction raw material inlet 21 of the fluidized bed reactor 2 and the reaction raw material outlet 12 of the vaporizer 1. In general, the vaporizer 1 heats and vaporizes a liquid reaction raw material, and then leads the liquid reaction raw material out of the reaction raw material outlet 12, and then enters the inside of the superheater 3 through the material inlet in the superheater 3, and further heats the reaction raw material to a predetermined temperature through the superheater 3, and then leads the liquid reaction raw material out of the material outlet in the superheater 3, and enters the inside of the fluidized bed reactor 2 through the reaction raw material inlet 21 of the fluidized bed reactor 2. The preset temperature can be generally determined according to the reaction temperature of the synthesis reaction in the fluidized bed reactor 2, for example, the preset temperature is set to be slightly lower or higher than the reaction temperature, so as to facilitate the subsequent synthesis reaction.
A synthesis product outlet 22 may also be included in the fluidized bed reactor 2 such that synthesis product produced by the synthesis reaction is conducted away from the synthesis product outlet 22.
In practical applications, for the synthesis product led out from the synthesis product outlet 22, which may also contain catalyst or other solid substances, a cyclone 4 and a washing tower 5 may be additionally provided in the material synthesis system 100, and the synthesis product outlet 22 of the fluidized bed reactor 2 is connected to the material inlet 41 of the cyclone 4, so that the synthesis product is introduced into the cyclone 4 from the material inlet 41, and the gas phase and the solid phase are separated by the cyclone 4.
Since the solid phase separated by the cyclone 4 is usually a catalyst or some solid reaction material, the solid phase outlet 43 of the cyclone 4 may be connected to the recovery unit B for recovery. As for the gas phase separated by the cyclone 4, which contains a large amount of synthesis product, the gas phase outlet 42 of the cyclone 4 may be connected to the material inlet 51 of the scrubber 5, so that the gas phase separated by the cyclone 4 is introduced into the scrubber 5 and purified by the scrubber 5, thereby obtaining the final purified synthesis product.
In the cyclone 4, the material inlet 41 may be generally provided on the sidewall of the lower end, the gas phase outlet 42 may be provided on the top, and the solid phase outlet 43 may be provided on the bottom.
The material inlet 51 of the washing column 5 is usually provided at the bottom of the washing column 5, so that the gas phase separated by the cyclone 4 is introduced into the washing column 5, and after the gas phase is purified by the washing column 5, the purified gas phase is further led out from the gas phase material outlet 54 of the washing column 5, so that the purified synthesis product is obtained, and the gas phase material outlet 54 may be connected to the synthesis product transport pipe C, so that the purified synthesis product is transported to a designated storage device. The gas phase feed outlet 54 can be generally disposed at the top of the scrubber 5 to facilitate the export of the purified synthesis product.
A liquid phase feed outlet 52 may be included in the scrubber 5 to remove liquid phase feed therefrom. In practical applications, since the liquid-phase material discharged from the liquid-phase material outlet 52 may contain a large amount of reaction raw materials, synthesis products, and the like, the material synthesis system 100 may further include an evaporator 6, and the material inlet 61 of the evaporator 6 is connected to the liquid-phase material outlet 52, so that the liquid-phase material discharged from the liquid-phase material outlet 52 is introduced into the evaporator 6, the liquid-phase material is heated and evaporated by the evaporator 6, and the gas-phase material obtained by evaporation is discharged from the gas-phase material outlet 62 of the evaporator 6, and the gas-phase material contains a large amount of reaction raw materials, synthesis products, and the like, and can be recycled.
The gas-phase material discharged from the gas-phase material outlet 62 of the evaporator 6 may be reintroduced into the scrubber 5, purified by the scrubber 5, and then discharged from the gas-phase material outlet 54 of the scrubber 5. For example, a recycle inlet 53 may be additionally provided in the scrubber 5, and the recycle inlet 53 may be connected to the gas material outlet 62 of the evaporator 6, so as to recycle the gas material discharged from the gas material outlet 62 of the evaporator 6.
It is also possible to provide a second material inlet 63 in the evaporator 6 so that the drain outlet 13 is connected to the second material inlet 63 via a connecting pipe, so that easily clogged substances discharged from the drain outlet 13 can be further heated in the evaporator 6 to evaporate the reaction raw materials therefrom for recovery. In order to control the process of the easy-to-block substances discharged from the sewage draining outlet 13 flowing into the evaporator 6, a flow meter D and an adjusting valve E can be arranged in a connecting pipeline between the sewage draining outlet 13 and the second material inlet 63, the flow of the easy-to-block substances is measured by the flow meter D, and the flow rate or the connection and the disconnection of the connecting pipeline are controlled by the adjusting valve E. Of course, it is also possible to provide a sampling point F in the connecting line, so that a sample is taken via this sampling point F for the analysis of the composition and content of the substance in the connecting line.
The positions of the liquid-phase material outlet 52 and the recovered material inlet 53 in the washing column 5 may be generally set on the side wall of the lower end of the washing column 5. And the gas-phase material outlet 62 of the evaporator 6 can be arranged at the upper end of the evaporator 6, such as at the top of the evaporator 6, or at the side wall of the upper end; both the material inlet 61 and the second material inlet 63 in the evaporator 6 may be provided in the bottom or lower side wall of the evaporator 6, or may be provided in the top of the evaporator 6 and introduced into the lower end of the evaporator 6 through a pipe inserted into the lower end of the evaporator 6.
Based on the material synthesis system 100 provided in the embodiment of the present application, a material synthesis method may also be provided, where the method includes: in the process of synthesizing the material by using the material synthesizing system 100, the easily-clogged substances in the reaction raw materials are discharged by using the drain outlet 13 in the vaporizer 1. On one hand, the easily blocked substances in the reaction raw materials are discharged by utilizing the sewage outlet 13, so that the amount of the easily blocked substances entering the fluidized bed reactor 2 is reduced; on the other hand, the easily-blocked substances are discharged by the sewage outlet 13 in the material synthesis process, so that continuous production can be continuously carried out without stopping the machine, and the production efficiency can be improved.
Of course, the specific manner of discharging the easily clogged substances in the reaction raw material by using the drain outlet 13 in the vaporizer 1 can be performed according to actual needs. For example, in the continuous production process, because the components of the reaction raw materials are relatively stable, the easily-clogged substances in the reaction raw materials can be discharged periodically by using the drain outlet 13 in the vaporizer 1, and the easily-clogged substances in the reaction raw materials can be discharged by using the drain outlet 13 every 1 week, 1 day, 3 days, 8 hours or other time periods; in some cases, the content of the easily-clogged substance in the reaction raw material in the vaporizer 1 may also be detected, and when the content exceeds a preset threshold, the easily-clogged substance is discharged through the drain outlet 13, for example, a sampling point F (the sampling point F may be connected to a sampling pipe) may be used for sampling analysis, so as to detect and obtain the content of the easily-clogged substance in the reaction raw material in the vaporizer 1. The preset threshold value can be usually set according to actual conditions, and when the content of the easily-blocked substances exceeds the preset threshold value, it indicates that the content of the easily-blocked substances is too high, and more easily-blocked substances enter the subsequent fluidized bed reactor 2, so that the blocking of the distribution plate a is easily caused; alternatively, when the content of the blocking prone substance is lower than the preset threshold value, the distribution plate a is less likely to be blocked by the blocking prone substance in the reaction raw material.
By adopting the material synthesis method provided by the embodiment of the application, the problems in the prior art can be solved because the material synthesis method is based on the sampling device provided by the embodiment of the application, and the details are not repeated here.
The above is a specific description of the material synthesis system and the material synthesis method provided in the embodiments of the present application, and for the convenience of understanding, the system and the method may be described below with reference to specific examples. In this example, specifically, the synthesized material is methylchlorosilane, and the reaction material introduced through the reaction material inlet 11 in the vaporizer 1 is chloromethane; and a material synthesis system as shown in fig. 1 was employed.
In the synthesis process of methyl chlorosilane, high-boiling-point easily-blocked substances such as carbon tetrachloride in methyl chloride easily block a distribution plate A in a fluidized bed reactor 2. According to the material synthesizing system 100 provided by the embodiment of the present application, after methyl chloride is introduced through the reaction raw material inlet 11 in the vaporizer 1, methyl chloride is heated and vaporized in the vaporizer 1, and high boiling point easily-clogged substances such as carbon tetrachloride are mainly kept in the vaporizer 1 in a liquid state, so that they can be discharged through the drain outlet 13.
The vaporized chloromethane is led out from a reaction raw material outlet 12 of the vaporizer 1 and enters the superheater 3; after the vaporized methyl chloride is heated to a temperature close to the synthesis reaction in the superheater 3, the methyl chloride further enters the fluidized bed reactor 2 from a reaction raw material inlet 21 of the fluidized bed reactor 2, the gaseous methyl chloride rises to a distribution plate A to fully contact and react with silicon powder, the generated product (methyl chlorosilane) comprises a catalyst and unreacted methyl chloride and silicon powder, the product is led out from a synthesis product outlet 22 of the fluidized bed reactor 2 and enters the cyclone separator 4 through a material inlet 41 of the cyclone separator 4, then a gas phase and a solid phase are separated by the cyclone separator 4, the gas phase is led out through a gas phase outlet 42 and enters the washing tower 5, the solid phase mainly comprises the catalyst and the silicon powder, and the solid phase is led out through a solid phase outlet 43.
After the gas phase entering the scrubber 5 is purified by the scrubber 5, the purified gas-phase synthesis product can be led out from the gas-phase material outlet 54 of the scrubber 5 to the synthesis product conveying pipe C. And the liquid phase material is led out from the liquid phase material outlet 52 in the washing tower 5 and is led into the evaporator 6 through the material inlet 61 of the evaporator 6, so that the methyl chlorosilane and the methyl chloride in the liquid phase material are evaporated and are led into the washing tower 5 from the reclaimed material inlet 53 of the washing tower 5 for recycling.
In addition, for the high boiling point easily clogged substance such as carbon tetrachloride which is led out from the drain outlet 13 and contains a certain amount of methyl chloride, the easily clogged substance can be led into the evaporator 6 through the connecting pipe, the methyl chloride in the easily clogged substance is further evaporated, and the easily clogged substance is led into the washing tower 5 through the recovered material inlet 53.
During the synthesis, samples may be taken at sample point F for analysis to determine whether to derive a blocking-prone substance, or to periodically derive a blocking-prone substance.
It is to be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in the process, method, article, or apparatus that comprises the element.
The above are merely examples of the present application and are not intended to limit the present application. Various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the scope of the claims of the present application.
Claims (10)
1. A material synthesis system, comprising: a vaporizer (1) and a fluidized bed reactor (2), wherein:
the vaporizer (1) is internally provided with a reaction raw material inlet (11), a reaction raw material outlet (12) and a drain outlet (13) for discharging easily blocked substances in the reaction raw materials; and the number of the first and second groups,
a reaction raw material inlet (21) in the fluidized bed reactor (2) is connected with a reaction raw material outlet (12) in the vaporizer (1).
2. The material synthesis system according to claim 1, characterized in that the blow-off outlet (13) is arranged at the bottom of the vaporizer (1); or the like, or, alternatively,
the sewage draining outlet (13) is arranged on the side wall of the lower end of the vaporizer (1).
3. The material synthesis system of claim 1, further comprising a superheater (3), wherein:
the superheater (3) is arranged in a connecting pipeline between a reaction raw material inlet (21) of the fluidized bed reactor (2) and a reaction raw material outlet (12) of the vaporizer (1).
4. The material synthesis system of claim 1, further comprising a cyclone (4) and a scrubber (5);
the synthetic product outlet (22) of the fluidized bed reactor (2) is connected with the material inlet (41) of the cyclone separator (4); and the number of the first and second groups,
the gas phase outlet (42) of the cyclone separator (4) is connected with the material inlet (51) of the washing tower (5).
5. The material synthesis system of claim 4, further comprising an evaporator (6); the washing tower (5) also comprises a liquid phase material outlet (52) and a reclaimed material inlet (53);
the liquid phase material outlet (52) in the washing tower (5) is connected with the material inlet (61) of the evaporator (6); and the number of the first and second groups,
the recycled material inlet (53) in the washing tower (5) is connected with the gas phase material outlet (62) of the evaporator (6).
6. The material synthesis system according to claim 5, characterized in that the evaporator (6) further comprises a second material inlet (63) connected to the blow-off outlet (13).
7. The material synthesis system as claimed in claim 6, characterized in that a flow meter and a regulating valve are arranged in the connecting pipe between the sewage drain (13) and the second material inlet (63).
8. The material synthesis system as claimed in claim 6, characterized in that a sampling point is provided in the connecting pipe between the sewage drain (13) and the second material inlet (63); and the number of the first and second groups,
the sampling point is connected with a sampling pipeline.
9. The material synthesis system of claim 4,
the solid phase outlet (43) of the cyclone separator (4) is connected with a recovery device; and the number of the first and second groups,
the gas phase material outlet (54) of the washing tower (5) is connected with a synthetic product conveying pipeline.
10. The material synthesis system according to claim 4, characterized in that the synthesis product outlet (22) in the fluidized bed reactor (2) is provided at the upper end of the fluidized bed reactor (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023120597.3U CN214681632U (en) | 2020-12-22 | 2020-12-22 | Material synthesis system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023120597.3U CN214681632U (en) | 2020-12-22 | 2020-12-22 | Material synthesis system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214681632U true CN214681632U (en) | 2021-11-12 |
Family
ID=78558994
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202023120597.3U Active CN214681632U (en) | 2020-12-22 | 2020-12-22 | Material synthesis system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214681632U (en) |
-
2020
- 2020-12-22 CN CN202023120597.3U patent/CN214681632U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2661985C (en) | Silicon production with a fluidized bed reactor integrated into a siemens-type process | |
| CN109987608B (en) | Method for simultaneously producing electronic-grade dichlorosilane, electronic-grade trichlorosilane and electronic-grade silicon tetrachloride | |
| KR101397349B1 (en) | Process for continuously producing monosilane | |
| AU2007331688B2 (en) | Method for producing acetone cyanhydrin and the subsequent products thereof by specific cooling | |
| KR20110067093A (en) | Fluidized bed reactor, the use thereof, and a method for the energy-independent hydration of chlorosilanes | |
| AU2007327788A1 (en) | Integrated process and apparatus for preparing esters of methacrylic acid from acetone and hydrocyanic acid | |
| KR101497719B1 (en) | Process and apparatus for preparing alkyl esters of methacrylic acid | |
| US8143434B2 (en) | Production by distillation of acetone cyanhydrin and method for producing methacrylic ester and subsequent products | |
| CN110743470A (en) | Gas-liquid phase chloroethylene production device and process | |
| AU2007331689B2 (en) | Method for producing methacrylic alkyl esters by way of azeotropic distillation | |
| CN107056582A (en) | Coal-ethylene glycol carbonylation system reclaims the system and method for methyl nitrite | |
| CN102076607A (en) | Methods for increasing polycrystalline silicon reactor productivity by recycle of silicon fines | |
| KR101439573B1 (en) | Method for the adsorptive purification of alkyl methacrylates | |
| CN214681632U (en) | Material synthesis system | |
| CN112495314A (en) | Material synthesis system and material synthesis method | |
| CN113461521B (en) | Production process system and production method of dialkyl maleate | |
| CN202808393U (en) | Vertical reverse flow fluorination furnace for producing tungsten hexafluoride | |
| CN105060297A (en) | Method and apparatus for producing trichlorosilane | |
| CN113548941A (en) | Synthesis method and device of methane chloride | |
| CN113845542A (en) | Method and system for removing ethyl hydride in crude dimethyldichlorosilane | |
| CN112174996B (en) | Method and device for continuously producing silane coupling agent | |
| HU197855B (en) | Process for producing chlorothioformiates in charged tube-nest reactors | |
| US4208530A (en) | Process for the recovery of atactic polymers | |
| CN204039071U (en) | Prepare the device of trichlorosilane | |
| CN103228664B (en) | Hydrochlorination heater and correlation technique thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |