Rectification system for anti-disproportionation reaction
By employing a mixing path and a static mixer heater to process materials in the disproportionation reaction, and by setting up multiple fixed beds and catalyst drying tanks, the efficiency and safety issues in traditional disproportionation reactions have been solved, achieving more efficient polysilicon production.
Patent Information
- Application Number
- CN202423046044.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-11
- Publication Date
- 2026-01-30
- Estimated Expiration
- 2034-12-11
AI Technical Summary
Traditional disproportionation reactions in polysilicon production have problems with reaction efficiency, separation efficiency, catalyst management complexity and safety, especially limitations in mass and heat transfer efficiency, uneven gas-liquid distribution, and the need to shut down the tower for catalyst replacement.
The system employs first and second mixing paths to process materials from different sources, precisely controls reaction conditions through static mixers and heaters, sets up multiple fixed beds and catalyst drying tanks, utilizes a unified steam pipeline network to supply steam, and includes an exhaust gas channel to improve reaction efficiency and safety.
It improves reaction efficiency and product quality, reduces operational complexity and energy consumption, enhances system safety, simplifies catalyst management, and ensures production stability and safety.
Smart Images
Figure CN223846878U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The present application relates to the technical field of reactive distillation, specifically to the technical field of a distillation system for disproportionation reaction. BACKGROUND
[0002] In the traditional polysilicon production process, the disproportionation reaction of dichlorosilane (DCS) and silicon tetrachloride (STC) is usually carried out in a disproportionation column, where the material directly enters the column and the reaction and separation processes are completed simultaneously. Although this method simplifies the process, it also has some limitations and deficiencies:
[0003] Reaction efficiency problem: The disproportionation reaction carried out in the column may be limited by mass transfer and heat transfer efficiency, resulting in suboptimal reaction conversion and product purity.
[0004] Separation efficiency problem: Due to the separation of the material in the column, the column plate efficiency and uneven gas-liquid distribution may affect the separation efficiency, thereby affecting the product purity.
[0005] Catalyst management problem: In the traditional process, catalyst replacement and regeneration often require the column to be stopped, which not only increases the operation difficulty but also may cause production interruption and efficiency reduction.
[0006] Safety and stability problem: Due to the complexity of the material in the column and the exothermic reaction, improper management may increase the safety risk, and the control requirements for the temperature and pressure in the column are high, affecting the stability of the system. SUMMARY
[0007] In order to solve the problem of uneven gas-liquid distribution in the prior art and the problem of complex catalyst replacement process requiring column replacement.
[0008] According to the present application, a distillation system for disproportionation reaction is provided, comprising:
[0009] A first mixing path, the inlet end of the first mixing path is connected to the outlet of the adsorption buffer tank and the outlet end of the first disproportionation column, and the outlet end of the first mixing path is connected to a hydrogenation disproportionation assembly;
[0010] A second mixing path, the inlet end of the second mixing path is connected to the outlet of the reduction column and the outlet end of the second disproportionation column, and the outlet end of the second mixing path is connected to a reduction disproportionation assembly;
[0011] The outlet end of the hydrogenation disproportionation assembly is connected to a primary distillation unit and a secondary distillation unit;
[0012] The outlet end of the reduction disproportionation assembly is connected to the primary distillation unit and the secondary distillation unit.
[0013] Further, the first mixing path further comprises a first static mixer and a first heater; the first static mixer is connected to the outlet of the adsorption buffer tank and the outlet end of the first reverse disproportionation tower, and the outlet end of the first static mixer is connected to the inlet end of the first heater.
[0014] Further, the outlet end of the first heater is connected to the hydrogenation reverse disproportionation assembly.
[0015] Further, the second mixing path further comprises a second static mixer and a second heater; the second static mixer is connected to the outlet of the reduction tower and the outlet end of the second reverse disproportionation tower, and the outlet end of the second static mixer is connected to the inlet end of the second heater.
[0016] Further, the outlet end of the second heater is connected to the reduction reverse disproportionation assembly.
[0017] Further, the hydrogenation reverse disproportionation assembly comprises a plurality of hydrogenation reverse disproportionation fixed beds, the inlet end of each hydrogenation reverse disproportionation fixed bed is connected to the outlet end of the first heater, and the outlet end of each hydrogenation reverse disproportionation fixed bed is respectively connected to the primary rectification unit and the secondary rectification unit.
[0018] Further, the reduction reverse disproportionation assembly comprises a plurality of reduction reverse disproportionation fixed beds, the inlet end of each reduction reverse disproportionation fixed bed is connected to the outlet end of the second heater, and the outlet end of each reduction reverse disproportionation fixed bed is respectively connected to the primary rectification unit and the secondary rectification unit.
[0019] Further, a plurality of catalyst drying tanks are further included, all the catalyst drying tanks are communicated to all the hydrogenation reverse disproportionation fixed beds and all the reduction reverse disproportionation fixed beds.
[0020] Further, a steam pipe network is further included, the steam pipe network is communicated to the first heater and the second heater.
[0021] Further, the outlet end of all the hydrogenation reverse disproportionation fixed beds and all the reduction reverse disproportionation fixed beds is further connected with a tail gas discharge channel.
[0022] Compared with the prior art, the beneficial results of the utility model lie in that:
[0023] The utility model can more accurately control the reaction condition, so as to improve the overall reaction efficiency by respectively pretreating the materials of different sources in the first mixing path and the second mixing path.
[0024] The utility model discloses a precise control two heater's temperature, and use steam pipe network unified supply steam can reduce energy loss, realize more efficient energy utilization.
[0025] The utility model discloses a first mixed road and a plurality of hydrogenation reverse disproportionation fixed bed are set up, and the second mixed road and the reduction reverse disproportionation fixed bed are handled the material of different impurity content respectively, simplify the processing flow, reduce the complexity of operation, guarantee the product quality simultaneously.
[0026] The utility model discloses a plurality of points set up catalyst drying jar, can replace catalyst in time, reduced the complexity of operation.
[0027] The utility model discloses a tail gas discharge channel setting, enhanced the security of system, is convenient for in time processing tail gas, reduced the potential security risk. BRIEF DESCRIPTION OF DRAWINGS
[0028] Other features, objects and advantages of the application will become more apparent from the following detailed description of non-limiting embodiments, read in conjunction with the accompanying drawings:
[0029] Figure 1 It is the flow chart of a rectification system for reverse disproportionation reaction according to the application.
[0030] First mixed road 1
[0031] Adsorption buffer tank 11
[0032] First reverse disproportionation tower 12
[0033] Hydrogenation reverse disproportionation component 13
[0034] First stage rectification unit 131
[0035] Second stage rectification unit 132
[0036] Second mixed road 2
[0037] Reduction tower 21
[0038] Second reverse disproportionation tower 22
[0039] Reduction reverse disproportionation component 23
[0040] First static mixer 14
[0041] First heater 15
[0042] Hydrogenation reverse disproportionation fixed bed (R01~R02)
[0043] Second static mixer 24
[0044] Second heater 25
[0045] Reduction-disproportionation fixed bed (R03~R05)
[0046] Catalyst drying tank 3
[0047] Steam pipe network 4 DETAILED DESCRIPTION
[0048] The application will be further described below in conjunction with the drawings and embodiments. It can be understood that the specific embodiments described herein are only used to explain the related utility model, and not limit the utility model. In addition, it should be noted that, for the convenience of description, only the parts related to the utility model are shown in the drawings.
[0049] It should be noted that the embodiments in the present application and the features in the embodiments can be combined with each other without conflict. The present application will be described in detail below with reference to the drawings and in conjunction with the embodiments.
[0050] As shown in Figure 1 A rectification system for disproportionation reaction, comprising:
[0051] The first mixed path 1 is connected to the outlet of the adsorption buffer tank 11 and the outlet end of the first disproportionation tower 12, and the outlet end of the first mixed path 1 is connected to the hydrogenation disproportionation assembly 13.
[0052] The second mixed path 2 is connected to the outlet of the reduction tower 21 and the outlet end of the second disproportionation tower 22, and the outlet end of the second mixed path 2 is connected to the reduction disproportionation assembly 23.
[0053] The outlet end of the hydrogenation disproportionation assembly 13 is connected to the first rectification unit 131 and the second rectification unit 132.
[0054] The outlet end of the reduction disproportionation assembly 23 is connected to the first rectification unit 131 and the second rectification unit 132.
[0055] The utility model discloses a first mixed path 1 and second mixed path 2 are set up, and DCS (dichlorodihydrogen silicon) from the outlet of adsorption buffer tank 11 and STC (silicon tetrachloride) from the outlet of first disproportionation tower 12 are mixed, and dichlorodihydrogen silicon from reduction tower 21 and silicon tetrachloride from second disproportionation tower 22 are mixed simultaneously, so that the material from different sources is treated respectively, because,
[0056] The impurity content of the material from adsorption buffer tank 11 and first disproportionation tower 12 is high, and the impurity content of the material from reduction tower 21 and second disproportionation tower 22 is low, so that different temperature reaction treatment can be carried out, and energy loss and treatment complexity are reduced under the condition of ensuring quality.
[0057] In a preferred embodiment, the first mixing path 1 further comprises a first static mixer 14 and a first heater 15; the first static mixer 14 is connected to the outlet of the adsorption buffer tank 11 and the outlet end of the first dehydrochlorination tower 12, and the outlet end of the first static mixer 14 is connected to the inlet end of the first heater 15. The first static mixer 14 is used to mix the fluid from the outlet of the adsorption buffer tank 11 and the outlet of the first dehydrochlorination tower 12. The static mixer is a high-efficiency mixing device without moving parts, and its basic working mechanism is to change the flow state of the fluid in the pipe by using mixing unit bodies fixed in the pipe, so as to produce cutting, shearing, rotation and re-mixing between different fluids, so as to achieve the purpose of good dispersion and sufficient mixing; the first heater 15 uses steam heating, can accurately control the heating temperature, and ensures that the reaction is carried out under the best conditions.
[0058] In a preferred embodiment, the outlet end of the first heater 15 is connected to the hydrogenation dehydrochlorination assembly 13. The outlet end of the first heater 15 is directly connected to the hydrogenation dehydrochlorination assembly 13, which ensures that the heated fluid can quickly and efficiently enter the reaction assembly to carry out the hydrogenation dehydrochlorination reaction.
[0059] In a preferred embodiment, the hydrogenation dehydrochlorination assembly 13 comprises a plurality of hydrogenation dehydrochlorination fixed beds (R01~R02), and the inlet end of each hydrogenation dehydrochlorination fixed bed (R01~R02) is connected to the outlet end of the first heater 15, and the outlet end of each hydrogenation dehydrochlorination fixed bed (R01~R02) is respectively connected to the first rectification unit 131 and the second rectification unit 132. The hydrogenation dehydrochlorination assembly 13 is composed of a plurality of hydrogenation dehydrochlorination fixed beds (R01~R02), which allows multiple parallel reaction paths, thereby improving the reaction capacity and processing efficiency of the entire system.
[0060] The process of the first mixing path 1 starts as follows: the DCS feed amount of the outlet of the adsorption buffer tank 11 is 7.4t / h, and the STC feed amount of the outlet of the first dehydrochlorination tower 12 is 20t / h; after mixing in the first static mixer 14, the mixture is heated to 60-80℃ by the first heater 15 (steam heating, 134℃, 0.2MPaG, from the steam pipe network), and then enters the hydrogenation dehydrochlorination fixed bed (R01~R02) (DCS processing capacity is 10t / h, and STC processing capacity is 40t / h), and under the action of the catalyst, trichlorosilane is generated; then the reacted product enters the first rectification unit and the second rectification unit, respectively. The first rectification unit is responsible for recycling and converting dichlorodihydrogen silicon generated in the synthesis, reduction and hydrogenation processes of trichlorosilane. The main principle is to convert dichlorodihydrogen silicon and silicon tetrachloride into trichlorosilane in the disproportionation reactor through the action of the catalyst. The second rectification unit further purifies trichlorosilane.
[0061] In a preferred embodiment, the second mixing section 2 further comprises a second static mixer 24 and a second heater 25; the second static mixer 24 is connected to the outlet of the reduction column 21 and the outlet end of the second reverse disproportionation column 22, and the outlet end of the second static mixer 24 is connected to the inlet end of the second heater 25. The second static mixer 24 is used to mix the fluids from the outlet of the reduction column 21 and the outlet end of the second reverse disproportionation column 22. The static mixer is a kind of mixing device without moving parts, which can realize the mixing of fluids by the mixing units fixed in the pipe, through the splitting, merging and rotating of the fluids in the flow process. The outlet end of the second static mixer 24 is connected to the inlet end of the second heater 25, and the second heater 25 is used to heat the mixed fluids to a suitable temperature to meet the needs of the subsequent reverse disproportionation reaction.
[0062] In a preferred embodiment, the outlet end of the second heater 25 is connected to the reduction reverse disproportionation assembly 23, which is used to heat the mixed fluids from the second static mixer 24 (if present) to a suitable temperature to meet the needs of the subsequent reverse disproportionation reaction. The second heater 25 is used to heat the mixed fluids from the second static mixer 24 to a suitable temperature. This step is critical because the reverse disproportionation reaction usually needs to be carried out under specific temperature conditions to ensure the efficiency of the reaction and the quality of the product.
[0063] In a preferred embodiment, the reduction reverse disproportionation assembly 23 comprises a plurality of reduction reverse disproportionation fixed beds (R03~R05), and the inlet end of each reduction reverse disproportionation fixed bed (R03~R05) is connected to the outlet end of the second heater 25, and the outlet end of each reduction reverse disproportionation fixed bed (R03~R05) is connected to a primary rectification unit and a secondary rectification unit, respectively. The inlet end of each reduction reverse disproportionation fixed bed (R03~R05) is directly connected to the outlet end of the second heater 25, which ensures that the heated fluids can be quickly and uniformly distributed to each reaction bed. At the same time, the outlet end of each reduction reverse disproportionation fixed bed (R03~R05) is connected to a primary rectification unit and a secondary rectification unit, respectively, which allows the reaction products to directly enter the subsequent process.
[0064] In a preferred embodiment, it further comprises a plurality of catalyst drying tanks 3, all of which are connected to all of the hydrogenation reverse disproportionation fixed beds (R01~R02) and all of the reduction reverse disproportionation fixed beds (R03~R05). All of the catalyst drying tanks 3 are connected to all of the hydrogenation reverse disproportionation fixed beds (R01~R02) and all of the reduction reverse disproportionation fixed beds (R03~R05). This connection structure allows the catalyst to move flexibly between the drying tank and the reaction bed, which is convenient for the replacement and regeneration of the catalyst; through the use of the catalyst drying tank 3, the catalyst can be properly dried before entering the reaction bed, which improves the activity of the catalyst and the efficiency of the reaction.
[0065] In a preferred embodiment, a steam pipe network 4 is further included, which is connected to the first heater 15 and the second heater 25. The steam pipe network 4 is connected to the first heater 15 and the second heater 25, which ensures that the heaters can obtain a continuous and stable steam supply. In addition, the steam pipe network 4 can adjust the steam pressure and flow according to actual needs to adapt to different reaction requirements.
[0066] In a preferred embodiment, the outlet ends of all the hydrogenative re-disproportionation fixed beds (R01~R02) and all the reductive re-disproportionation fixed beds (R03~R05) are further connected with tail gas discharge channels.
[0067] The above description is only a preferred embodiment of the present application and an explanation of the technical principles applied. Those skilled in the art should understand that the utility model range involved in the present application is not limited to the technical solutions formed by the specific combination of the above technical features, and should also cover other technical solutions formed by any combination of the above technical features or equivalent features without departing from the above utility model concept. For example, the above features are replaced with the technical features disclosed in the present application (but not limited to) having similar functions to form technical solutions.
Claims
1. A rectification system for a disproportionation reaction, characterized in that, Comprising of: a first mixing line, the inlet end of which is connected to the outlet from the adsorption buffer tank and the outlet end of the first dehydrogenation tower, the outlet end of which is connected to the hydrogenation dehydrogenation assembly; a second mixing line, the inlet end of which is connected to the outlet from the reduction tower and the outlet end of the second dehydrogenation tower, the outlet end of which is connected to the reduction dehydrogenation assembly; the outlet end of the hydrogenation dehydrogenation assembly is connected to the primary rectification unit and the secondary rectification unit; the outlet end of the reduction dehydrogenation assembly is connected to the primary rectification unit and the secondary rectification unit.
2. The rectification system for a retro-disproportionation reaction according to claim 1, wherein The first mixing line further comprises a first static mixer and a first heater; the first static mixer is connected to the outlet from the adsorption buffer tank and the outlet end of the first dehydrogenation tower, the outlet end of the first static mixer is connected to the inlet end of the first heater.
3. The rectification system for a retro-disproportionation reaction according to claim 2, wherein The outlet end of the first heater is connected to the hydrogenation dehydrogenation assembly.
4. The rectification system for a retro-disproportionation reaction according to claim 1, wherein The second mixing line further comprises a second static mixer and a second heater; the second static mixer is connected to the outlet from the reduction tower and the outlet end of the second dehydrogenation tower, the outlet end of the second static mixer is connected to the inlet end of the second heater.
5. The rectification system for a retro-disproportionation reaction according to claim 4, wherein The outlet end of the second heater is connected to the reduction dehydrogenation assembly.
6. The rectification system for a retro-disproportionation reaction according to claim 2, wherein The hydrogenation dehydrogenation assembly comprises a plurality of hydrogenation dehydrogenation fixed beds, the inlet end of each of the hydrogenation dehydrogenation fixed beds is connected to the outlet end of the first heater, and the outlet end of each of the hydrogenation dehydrogenation fixed beds is respectively connected to the primary rectification unit and the secondary rectification unit.
7. The rectification system for a retro-disproportionation reaction according to claim 4, wherein The reduction dehydrogenation assembly comprises a plurality of reduction dehydrogenation fixed beds, the inlet end of each of the reduction dehydrogenation fixed beds is connected to the outlet end of the second heater, and the outlet end of each of the reduction dehydrogenation fixed beds is respectively connected to the primary rectification unit and the secondary rectification unit.
8. A rectifying system for a retro-disproportionation reaction according to claim 6 or 7, characterized in that, Further comprising of: a plurality of catalyst drying tanks, all of which are connected to all of the hydrogenation dehydrogenation fixed beds and all of the reduction dehydrogenation fixed beds.
9. The rectification system for a retro-disproportionation reaction according to claim 6 or 7, wherein Further comprising of: a steam pipe network, which is connected to the first heater and the second heater.
10. The rectification system for a retro-disproportionation reaction according to claim 6 or 7, wherein The outlet end of all of the hydrogenation dehydrogenation fixed beds and all of the reduction dehydrogenation fixed beds is further connected with a tail gas discharge channel.