CN219721944U - Rectification system for polysilicon production - Google Patents
Rectification system for polysilicon production Download PDFInfo
- Publication number
- CN219721944U CN219721944U CN202321204664.0U CN202321204664U CN219721944U CN 219721944 U CN219721944 U CN 219721944U CN 202321204664 U CN202321204664 U CN 202321204664U CN 219721944 U CN219721944 U CN 219721944U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- shell side
- outlet end
- tower
- reboiler
- 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
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 229910021420 polycrystalline silicon Inorganic materials 0.000 title claims abstract description 26
- 229920005591 polysilicon Polymers 0.000 title claims abstract description 23
- 238000007323 disproportionation reaction Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 239000007791 liquid phase Substances 0.000 claims abstract description 14
- 238000000605 extraction Methods 0.000 claims abstract description 10
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 239000012071 phase Substances 0.000 claims description 5
- 238000005984 hydrogenation reaction Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 18
- 239000000463 material Substances 0.000 description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000013459 approach Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical group C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000005049 silicon tetrachloride Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Silicon Compounds (AREA)
Abstract
The utility model discloses a polysilicon production rectification system, relates to the technical field of polysilicon production, and mainly aims to improve the thermal efficiency of a polysilicon production rectification process. The main technical scheme of the utility model is as follows: a polysilicon production rectification system comprising: the first-stage tower is connected to one end of the side line extraction pipeline; the second-stage tower is provided with a first reboiler, and the shell side inlet end of the first reboiler is connected with the other end of the side line extraction pipeline; the shell side inlet end of the first heat exchanger is connected to the shell side outlet end of the first reboiler, the shell side outlet end of the first heat exchanger is connected to the top wall of the buffer tank, the tube side inlet end of the first heat exchanger is connected to the reduction dry liquid phase recovery pipeline, the tube side outlet end of the first heat exchanger is connected to the shell side inlet end of the second heat exchanger, the shell side outlet end of the second heat exchanger is connected to the feed inlet of the first-stage tower, the bottom wall of the buffer tank is connected to the tube side inlet end of the second heat exchanger, and the tube side outlet end of the second heat exchanger is connected to the anti-disproportionation device.
Description
Technical Field
The utility model relates to the technical field of polysilicon production, in particular to a polysilicon production rectification system.
Background
The rectifying tower is widely used in chemical industry, including petrochemical industry, coal chemical industry, polysilicon industry, etc. The principle of the rectifying tower is that equipment for separating and purifying each component of the mixture is achieved through multiple vaporization and condensation according to the difference of the volatility of each component in the liquid mixture. Because of the difference of separation difficulty between different components, the number of tower plates or the height of packing of the rectifying towers is greatly different, the heights of the rectifying towers are also greatly different, and the heights are different from 20m to 120 m.
In the rectification section in the production of polysilicon, the side-produced material of the reduction primary tower is silicon tetrachloride, the production temperature is high, most enterprises mainly use circulating water for cooling the side-produced material of the reduction primary tower, the heat of the side-produced material of the reduction primary tower cannot be effectively recycled, and the consumption of circulating water is increased.
Disclosure of Invention
In view of this, the embodiment of the utility model provides a polysilicon production rectification system, which is mainly aimed at improving the thermal efficiency of the polysilicon production rectification process.
In order to achieve the above purpose, the present utility model mainly provides the following technical solutions:
the embodiment of the utility model provides a polysilicon production rectifying system, which comprises: the device comprises a primary tower, a secondary tower and a heat exchange part;
the primary tower is connected to one end of the side line extraction pipeline;
the second-stage tower is provided with a first reboiler, and the shell side inlet end of the first reboiler is connected with the other end of the side line extraction pipeline;
the heat exchange part comprises a first heat exchanger, a second heat exchanger and a buffer tank, wherein the shell side inlet end of the first heat exchanger is connected to the shell side outlet end of the first reboiler, the shell side outlet end of the first heat exchanger is connected to the top wall of the buffer tank, the tube side inlet end of the first heat exchanger is connected to a reduction dry liquid phase recovery pipeline, the tube side outlet end of the first heat exchanger is connected to the shell side inlet end of the second heat exchanger, the shell side outlet end of the second heat exchanger is connected to the feed inlet of the primary tower, the bottom wall of the buffer tank is connected to the inlet of a booster pump, and the outlet end of the booster pump is connected to the tube side inlet end of the second heat exchanger.
The aim and the technical problems of the utility model can be further realized by adopting the following technical measures.
Optionally, the device further comprises a third heat exchanger, wherein the outlet end of the booster pump is connected with the shell side inlet end of the third heat exchanger, the shell side outlet end of the third heat exchanger is connected with the cold hydrogenation reactor, the tube side inlet end of the third heat exchanger is connected with the reduction dry gas-phase recovery material pipeline, and the tube side outlet end of the third heat exchanger is connected with the feed inlet of the primary tower.
Optionally, the air pre-cooler is further included, and the tube side outlet end of the second heat exchanger, the air pre-cooler and the anti-disproportionation device are sequentially connected.
Optionally, the secondary tower is further provided with a steam reboiler.
Optionally, a flow meter and a regulating valve are further arranged in the pipeline between the second heat exchanger and the anti-disproportionation device.
Optionally, the device further comprises a filter, wherein the filter is arranged at an inlet pipeline of the booster pump.
By means of the technical scheme, the utility model has at least the following advantages:
the extracted material of the first-stage tower flows to the shell side of the reboiler through a side extraction pipeline, heats up the material at the bottom of the second-stage tower, flows through the shell side of the first heat exchanger, and finally flows into the buffer tank. In the first heat exchanger, the reduction dry liquid-phase reclaimed material absorbs heat of side-line reclaimed materials, the side-line reclaimed materials are condensed and liquefied in the buffer tank, the liquefied side-line reclaimed materials are pressurized by the booster pump and flow through the tube side of the second heat exchanger, the heat of the side-line reclaimed materials is further conducted to the reduction dry liquid-phase reclaimed material, and the side-line reclaimed materials finally enter the anti-disproportionation device; and the liquid phase reclaimed materials of the reduction dry method flowing out of the shell pass of the second heat exchanger enter a first-stage tower.
Through the process, the side offtake materials sequentially provide heat for the bottom materials of the secondary tower and the liquid-phase recovery materials of the reduction dry method, the temperature of the side offtake materials is reduced and approaches to the anti-disproportionation reaction temperature, and the use of circulating water for cooling the side offtake materials is avoided; the temperature of the liquid phase reclaimed material of the reduction dry method is raised before entering the primary tower, so that the temperature raising load of a reboiler of the primary tower is reduced.
In conclusion, the system improves the thermal efficiency of the polysilicon production rectification process.
Drawings
Fig. 1 is a schematic structural diagram of a rectification system for polysilicon production according to an embodiment of the present utility model.
Reference numerals in the drawings of the specification include: the system comprises a primary tower 1, a secondary tower 2, a side-draw pipeline 3, a first reboiler 4, a first heat exchanger 5, a second heat exchanger 6, a buffer tank 7, a third heat exchanger 8, a booster pump 9, an air precooler 10, a steam reboiler 11, a flowmeter 12, a regulating valve 13 and a filter 14.
Detailed Description
In order to further describe the technical means and effects adopted for achieving the preset aim of the utility model, the following detailed description refers to the specific implementation, structure, characteristics and effects according to the application of the utility model with reference to the accompanying drawings and preferred embodiments. In the following description, different "an embodiment" or "an embodiment" do not necessarily refer to the same embodiment. Furthermore, the particular features, structures, or characteristics of one or more embodiments may be combined in any suitable manner.
The utility model is described in further detail below with reference to the drawings and examples.
As shown in fig. 1, an embodiment of the present utility model provides a polysilicon production rectification system, which includes: the device comprises a primary tower 1, a secondary tower 2 and a heat exchange part;
the primary tower 1 is connected to one end of a side line extraction pipeline 3;
the secondary tower 2 is provided with a first reboiler 4, and the shell side inlet end of the first reboiler 4 is connected with the other end of the side extraction pipeline 3;
the heat exchange part comprises a first heat exchanger 5, a second heat exchanger 6 and a buffer tank 7, wherein the shell side inlet end of the first heat exchanger 5 is connected to the shell side outlet end of the first reboiler 4, the shell side outlet end of the first heat exchanger 5 is connected to the top wall of the buffer tank 7, the tube side inlet end of the first heat exchanger 5 is connected to a reduction dry liquid phase recovery material pipeline, the tube side outlet end of the first heat exchanger 5 is connected to the shell side inlet end of the second heat exchanger 6, the shell side outlet end of the second heat exchanger 6 is connected to the feed inlet of the first-stage tower 1, the bottom wall of the buffer tank 7 is connected to the inlet of a booster pump 9, the outlet end of the booster pump 9 is connected to the tube side inlet end of the second heat exchanger 6, and the tube side outlet end of the second heat exchanger 6 is connected to an anti-disproportionation device.
The working process of the polysilicon production rectifying system is as follows:
the extracted material of the primary tower 1 flows to the shell side of the reboiler through a side extraction pipeline 3, heats the material at the bottom of the secondary tower 2, flows to the shell side of the first heat exchanger 5, and finally flows into the buffer tank 7. In the first heat exchanger 5, the reduction dry liquid-phase reclaimed material absorbs heat of side-line reclaimed materials, the side-line reclaimed materials are condensed and liquefied in the buffer tank 7, the liquefied side-line reclaimed materials are pressurized by the booster pump 9 and flow through the tube side of the second heat exchanger 6, the heat of the side-line reclaimed materials is further conducted to the reduction dry liquid-phase reclaimed material, and the side-line reclaimed materials finally enter the anti-disproportionation device; the liquid phase recovery material of the reduction dry method flowing out of the shell pass of the second heat exchanger 6 enters the first-stage tower 1.
Through the process, the side offtake materials sequentially provide heat for the bottom materials of the secondary tower 2 and the liquid phase recovery materials of the reduction dry method, the temperature of the side offtake materials is reduced and approaches to the anti-disproportionation reaction temperature, and the use of circulating water for cooling the side offtake materials is avoided; the temperature of the liquid phase reclaimed material of the reduction dry method is raised before entering the primary tower 1, so that the temperature rise load of a reboiler of the primary tower 1 is reduced.
In the technical scheme of the utility model, the system improves the thermal efficiency of the polysilicon production rectification process.
Specifically, the first reboiler 4, the first heat exchanger 5 and the second heat exchanger 6 are respectively tube-array heat exchangers; the buffer tank 7 is a horizontal storage tank.
Specifically, in the process of deposition reaction in the polysilicon reduction furnace, the reaction conversion rate is low, most unreacted gas is discharged out of the reduction furnace through a chassis tail gas pipe, so that tail gas recovery is needed, the tail gas recovery material is a reduction dry recovery material, and the reduction dry recovery material is treated by a primary tower and a secondary tower to participate in the next reaction again, thereby reducing the production cost.
As shown in fig. 1, in the specific embodiment, the device further comprises a third heat exchanger 8, the outlet end of the booster pump 9 is connected to the shell side inlet end of the third heat exchanger 8, the shell side outlet end of the third heat exchanger 8 is connected to the cold hydrogenation reactor, the tube side inlet end of the third heat exchanger 8 is connected to the reduction dry gas-phase recovery material pipeline, and the tube side outlet end of the third heat exchanger 8 is connected to the feed inlet of the primary tower 1.
In this embodiment, specifically, part of the side offtake material is conveyed to the shell side of the third heat exchanger 8 by the booster pump 9, and in the third heat exchanger 8, the heat of the side offtake material is transferred to the recovery material in the gas phase of the reduction dry method, and after the heat exchange is completed, the recovery material in the gas phase of the reduction dry method enters the primary tower 1, and the side offtake material enters the cold hydrogenation reactor.
As shown in fig. 1, in a specific embodiment, the air pre-cooler 10 is further included, and the tube side outlet end of the second heat exchanger 6, the air pre-cooler 10 and the anti-disproportionation device are sequentially connected.
In this embodiment, in order to further make the temperature of the side offtake material approach the anti-disproportionation reaction temperature, the side offtake material flowing out of the second heat exchanger 6 is further cooled down by the air precooler 10 and then enters the anti-disproportionation reactor.
In a specific embodiment, as shown in fig. 1, the secondary column 2 is further provided with a steam reboiler.
In this embodiment, although the temperature of the first reboiler 4 can be raised by the side offtake material, the temperature difference between the side offtake material and the bottom material of the secondary tower 2 cannot raise the temperature of the bottom material of the secondary tower 2 to the temperature required by the process, so that the steam reboiler 11 is added as a supplement to the heat source of the bottom material of the secondary tower 2.
In the specific embodiment, as shown in fig. 1, the pipeline between the second heat exchanger 6 and the anti-disproportionation device is further provided with a flow meter 12 and a regulating valve 13.
In this embodiment, specifically, the flowmeter 12 and the regulating valve 13 are integrated in the DCS control system, and the side offcut material flows through the second heat exchanger 6, the flowmeter 12, the regulating valve 13 and the anti-disproportionation device in sequence, and an operator can specifically control the opening of the regulating valve 13 by means of DCS integral feedback control, so that the flow rate of the side offcut material meets the requirements of the anti-disproportionation reaction process.
In the specific embodiment, as shown in fig. 1, a filter 14 is further included, and the filter 14 is mounted to the inlet pipe of the booster pump 9.
In the present embodiment, specifically, in order to prevent impurities in the buffer tank 7 from flowing into the subsequent heat exchanger or reactor along with the side offtake, a filter 14 is installed to filter impurities in the buffer tank 7.
The foregoing is merely illustrative of the present utility model, and the present utility model is not limited thereto, and any person skilled in the art will readily recognize that variations or substitutions are within the scope of the present utility model. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.
Claims (7)
1. A polysilicon production rectification system, comprising:
the primary tower is connected to one end of the side line extraction pipeline;
the second-stage tower is provided with a first reboiler, and the shell side inlet end of the first reboiler is connected with the other end of the side line extraction pipeline;
the heat exchange part comprises a first heat exchanger, a second heat exchanger and a buffer tank, wherein the shell side inlet end of the first heat exchanger is connected with the shell side outlet end of the first reboiler, the shell side outlet end of the first heat exchanger is connected with the top wall of the buffer tank, the tube side inlet end of the first heat exchanger is connected with a reduction dry liquid phase recovery pipeline, the tube side outlet end of the first heat exchanger is connected with the shell side inlet end of the second heat exchanger, the shell side outlet end of the second heat exchanger is connected with the feed inlet of the primary tower, the bottom wall of the buffer tank is connected with the inlet of a booster pump, and the outlet end of the booster pump is connected with the tube side inlet end of the second heat exchanger which is connected with a disproportionation device.
2. The polysilicon production rectifying system according to claim 1, characterized in that,
the device comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, a first stage tower, a second stage tower, a third heat exchanger, a first stage tower and a second stage tower, wherein the outlet end of the booster pump is connected with the shell side inlet end of the third heat exchanger, the shell side outlet end of the third heat exchanger is connected with the cold hydrogenation reactor, the tube side inlet end of the third heat exchanger is connected with a reduction dry gas-phase recovery pipeline, and the tube side outlet end of the third heat exchanger is connected with the feed inlet of the first stage tower.
3. The polysilicon production rectifying system according to claim 1, characterized in that,
the air precooler is connected with the second heat exchanger in sequence.
4. The polysilicon production rectifying system according to claim 1, characterized in that,
the secondary tower is also provided with a steam reboiler.
5. The polycrystalline silicon production rectification system as claimed in any one of claims 1 to 4, wherein,
and a flow meter and a regulating valve are further arranged in the pipeline between the second heat exchanger and the anti-disproportionation device.
6. The polycrystalline silicon production rectification system as claimed in any one of claims 1 to 4, wherein,
the filter is arranged on an inlet pipeline of the booster pump.
7. The polycrystalline silicon production rectification system as claimed in any one of claims 1 to 4, wherein,
the shell side outlet end of the first reboiler is respectively connected with the shell side inlet end of the first heat exchanger and the top wall of the buffer tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321204664.0U CN219721944U (en) | 2023-05-18 | 2023-05-18 | Rectification system for polysilicon production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321204664.0U CN219721944U (en) | 2023-05-18 | 2023-05-18 | Rectification system for polysilicon production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219721944U true CN219721944U (en) | 2023-09-22 |
Family
ID=88051955
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321204664.0U Active CN219721944U (en) | 2023-05-18 | 2023-05-18 | Rectification system for polysilicon production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219721944U (en) |
-
2023
- 2023-05-18 CN CN202321204664.0U patent/CN219721944U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103896280B (en) | A kind of operation method of polysilicon cold hydrogenation | |
| CN111068465A (en) | Continuous absorption method for byproduct hydrogen chloride gas in chlorination reaction | |
| CN102267868B (en) | Industrial production apparatus for trichloroethylene | |
| CN100429194C (en) | Method for utilizing reaction heat in process of producing methane chloride and purifying mixture | |
| CN211514013U (en) | Continuous absorption device for byproduct hydrogen chloride gas in chlorination reaction | |
| CN210198116U (en) | Tail gas cooling device for gas washing tower of yellow phosphorus electric furnace | |
| CN219721944U (en) | Rectification system for polysilicon production | |
| CN208694295U (en) | A kind of polycrystalline silicon production line exhaust gas recovery system | |
| CN201762266U (en) | Trichloroethylene industrialized production device | |
| CN201855641U (en) | Device for treating tail gas containing hydrogen chloride | |
| CN208413844U (en) | The purifying plant of high yield super clean, high purified hydrofluoric acid | |
| CN217303696U (en) | Cold volume recycle system of cold hydrogenation in polycrystalline silicon production | |
| CN212988122U (en) | Heat energy recovery system suitable for cold hydrogenation technology | |
| CN202554976U (en) | Energy-saving and emission reduction distillation system | |
| CN1037087C (en) | Extruding fluorine absorbing process | |
| CN103991874A (en) | Method and system for purifying trichlorosilane from chlorosilane | |
| CN210215200U (en) | Device for separating methanol water by virtue of supergravity rectification and reaction coupling decompression | |
| CN101792679B (en) | Energy-saving method for vaporizing feed of propylene depolymerization oil tower by stepped utilization of low-temperature wastewater and device thereof | |
| CN215428945U (en) | Chloroethylene production device | |
| CN113121303B (en) | Chloroethylene production process and special device thereof | |
| CN109340578A (en) | A kind of liquefied gas purification devices and method | |
| CN212833624U (en) | Mixed hydrocarbon rectifying device | |
| CN217119360U (en) | Rectification recovery device | |
| CN203959830U (en) | Prepare the system of polysilicon and the system of purify trichlorosilane | |
| CN104003396B (en) | Prepare the method and system of polysilicon and the method and system of purify trichlorosilane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |