CN217894433U - Silicon tetrachloride conveying system - Google Patents
Silicon tetrachloride conveying system Download PDFInfo
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- CN217894433U CN217894433U CN202221734802.1U CN202221734802U CN217894433U CN 217894433 U CN217894433 U CN 217894433U CN 202221734802 U CN202221734802 U CN 202221734802U CN 217894433 U CN217894433 U CN 217894433U
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Abstract
The utility model discloses a silicon tetrachloride conveying system belongs to conveying equipment technical field in the polycrystalline silicon production, including one-level buffer tank and second grade buffer tank, the one-level buffer tank passes through pipeline I and connects the second grade buffer tank, is equipped with delivery pump I on the pipeline I, the one-level buffer tank is connected with silicon tetrachloride feeding pipeline, hydrogen pipeline I and exhaust gas pipe I, be connected with hydrogen pipeline II, exhaust gas pipe II and silicon tetrachloride emission pipeline on the second grade buffer tank, be equipped with delivery pump II on the silicon tetrachloride emission pipeline, solved the raw materials silicon tetrachloride's of the cold hydrogenation workshop section of polycrystalline silicon production technology among the prior art conveying system, the equipment cost that relates to is higher, the investment volume is big, and system operating efficiency is lower, problem that the running cost is high.
Description
Technical Field
The utility model belongs to the technical field of conveying equipment in the polycrystalline silicon production, concretely relates to silicon tetrachloride conveying system.
Background
In the production process of polycrystalline silicon, the device operation conditions related to the cold hydrogenation chemical industry section are high-temperature and high-pressure environment, the system pressure is usually 2.5 to 3.3MPa, and when the raw material silicon tetrachloride enters a cold hydrogenation system, the silicon tetrachloride is lifted to be more than 3.8MPa from 0.3 to 0.5MPa by using a shielding pump, so that the production requirement can be met. At present, the whole industry adopts a high-lift pump to lift silicon tetrachloride from 0.3 to 0.5MPa to 3.8MPa at one time, and the lift of the pump is 230 to 260m generally.
The shielding pump used at present can only use 380V or 690V low-voltage electricity because of the structure, which means that the power of a single pump can only reach 260kW at most, and if a pump with 230m of head is selected, the flow rate of the single pump can only reach 140 cubic meters. At present, with the development of the photovoltaic industry, the production scale of a polycrystalline silicon device is expanded to more than one hundred thousand tons at present from the original kiloton level, the feeding amount of silicon tetrachloride of a cold hydrogenation device is also increased by dozens of times, so that the number of silicon tetrachloride delivery pumps is greatly increased, the production requirement can be met by only 2 pumps at present, more than ten pumps are required at present, and three problems are caused after the number of the pumps is obviously increased:
1. after the number of the pumps is obviously increased, the probability of pump-out failure is greatly increased;
2. after the number of the pumps is increased, the corresponding equipment investment is also obviously increased;
3. the efficiency of high-lift pumps is often very low, resulting in high operating costs, which leads to the production cost of polycrystalline silicon still remaining at the level of the original process and being on the rise.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problems that in the prior art, the cost of the equipment is higher, the investment is large, the operation efficiency of the system is lower and the operation cost is high in a conveying system of raw material silicon tetrachloride for a cold hydrogenation section in a polysilicon production process.
In order to achieve the above purpose, the technical solution of the present invention is as follows:
the utility model provides a silicon tetrachloride conveying system, includes one-level buffer tank and second grade buffer tank, and the one-level buffer tank passes through pipeline I and connects the second grade buffer tank, is equipped with delivery pump I on the pipeline I, the one-level buffer tank is connected with silicon tetrachloride feed line, hydrogen pipeline I and exhaust gas pipe I, be connected with hydrogen pipeline II, exhaust gas pipe II and silicon tetrachloride discharge pipeline on the second grade buffer tank, be equipped with delivery pump II on the silicon tetrachloride discharge pipeline.
Furthermore, a pressure gauge I is arranged on the primary buffer tank, a regulating valve I is arranged on the exhaust gas pipe I, a regulating valve II is arranged on the hydrogen pipeline I, and the pressure gauge I is respectively in control connection with the regulating valve I and the regulating valve II.
Further, be equipped with pressure gauge II on the second grade buffer tank, be equipped with governing valve III on the exhaust pipe II, be equipped with governing valve IV on the hydrogen pipeline II, pressure gauge II respectively with governing valve III, governing valve IV control connection.
Furthermore, the secondary buffer tank is provided with a liquid level meter, a regulating valve V is arranged on the pipeline I, and the liquid level meter is connected with the regulating valve V in a control mode.
Further, the hydrogen line I is a 1.0MPa hydrogen line.
Further, the hydrogen pipeline II is a 2.4MPa hydrogen pipeline.
The utility model has the advantages that:
1. in the utility model, the silicon tetrachloride conveying system can ensure that the conveyed silicon tetrachloride reaches the pressure required by production, the lift of a single conveying pump can be reduced by a half, the efficiency of the conveying pump can be improved by more than 20 percent,the operation cost is obviously reduced; meanwhile, the flow of a single delivery pump can be increased by 3 times, and the flow of the single pump can reach 400m 3 By adopting the system design, the number of the delivery pumps can be reduced by half, and the production cost is obviously reduced.
2. In the utility model, a pressure gauge I is arranged on the primary buffer tank, a regulating valve I is arranged on the exhaust gas pipe I, a regulating valve II is arranged on the hydrogen pipeline I, and the pressure gauge I is respectively in control connection with the regulating valve I and the regulating valve II to control the opening and closing or the opening of the regulating valve I and the regulating valve II so as to keep the pressure of the primary buffer tank stable; in addition, be equipped with pressure gauge II on the second grade buffer tank, be equipped with governing valve III on the exhaust pipe II, be equipped with governing valve IV on the hydrogen pipeline II, respectively with governing valve III, governing valve IV control connection through pressure gauge II, thereby control governing valve III, governing valve IV's switching or aperture size realize that second grade buffer tank pressure keeps stable, realize automatically regulated, reduce the production management and control degree of difficulty.
3. The utility model discloses in, the second grade buffer tank is equipped with the level gauge, is equipped with governing valve V on the pipeline I, links to each other with governing valve V control through the level gauge, realizes that silicon tetrachloride's liquid level remains stable in the second grade buffer tank, guarantees the normal operating of equipment and the steady operation of technology.
4. In the utility model, the hydrogen pipeline I is a 1.0MPa hydrogen pipeline; the hydrogen pipeline II is a 2.4MPa hydrogen pipeline, and the pressure value which can reach the expectation of the silicon tetrachloride after secondary pressurization is ensured to meet the production requirement. Of course, in order to reduce the pressure of the delivery pump, the delivery system can be designed into more than two stages according to the scheme, but when a more multistage boosting system is designed, the more used devices and auxiliary pipelines are, the more difficult the device maintenance is, the higher the failure rate is, the higher the production cost is, and the purpose of the original design is not.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural diagram of another embodiment.
Wherein, 1, a first-stage buffer tank; 2. a secondary buffer tank; 3. a pipeline I; 4. a delivery pump I; 5. a silicon tetrachloride feed line; 6. a hydrogen line I; 7. an exhaust gas pipe I; 8. a hydrogen line II; 9. an exhaust pipe II; 10. a silicon tetrachloride discharge line; 11. a pressure gauge I; 12. adjusting a valve I; 13. adjusting a valve II; 14. a pressure gauge II; 15. adjusting a valve III; 16. adjusting a valve IV; 17. a liquid level meter; 18. adjusting a valve V; 19. and a delivery pump II.
Detailed Description
The present invention will be described in further detail with reference to examples, but the present invention is not limited thereto.
Example 1
The embodiment is the most basic embodiment, a silicon tetrachloride conveying system, belongs to conveying equipment technical field in the polycrystalline silicon production, including one-level buffer tank 1 and second grade buffer tank 2, refer to fig. 1, and one-level buffer tank 1 passes through pipeline I3 and connects second grade buffer tank 2, is equipped with delivery pump I4 on the pipeline I3, one-level buffer tank 1 is connected with silicon tetrachloride feed line 5, hydrogen pipeline I6 and exhaust gas pipe I7, be connected with hydrogen pipeline II8, exhaust gas pipe II9 and silicon tetrachloride emission pipeline 10 on the second grade buffer tank 2, be equipped with delivery pump II19 on the silicon tetrachloride emission pipeline 10.
When the system works, silicon tetrachloride from a rectification section in a polycrystalline silicon production process enters a primary buffer tank 1 from a silicon tetrachloride feeding pipeline 5, the pressure in the primary buffer tank 1 is balanced to a preset range value through a hydrogen pipeline I6 and an exhaust pipe I7, and then the pressure is pressurized for the first time to a certain pressure P1 through a delivery pump I4 and then is delivered to a secondary buffer tank 2 through a pipeline I3; the silicon tetrachloride of the secondary buffer tank 2 balances the pressure in the secondary buffer tank 2 to a preset range value through a hydrogen pipeline II8 and an exhaust pipe II9, and then is pressurized for the second time to a certain pressure P2 through a delivery pump II19 and then is delivered to the cold hydrogenation section.
Example 2
The present embodiment is further optimized in embodiment 1, except that a pressure gauge I11 is disposed on the primary buffer tank 1, a regulating valve I12 is disposed on the exhaust pipe I7, and a regulating valve II13 is disposed on the hydrogen pipe I6, and referring to fig. 2, the pressure gauge I11 is respectively in control connection with the regulating valve I12 and the regulating valve II 13.
Example 3
Compared with the embodiment 1-2, the present embodiment has the difference that the secondary buffer tank 2 is provided with a pressure gauge II14, the exhaust pipe II9 is provided with a regulating valve III15, the hydrogen pipe II8 is provided with a regulating valve IV16, and referring to fig. 2, the pressure gauge II14 is respectively in control connection with the regulating valve III15 and the regulating valve IV 16.
Example 4
Compared with the embodiments 1-3, the present embodiment has the difference that the secondary buffer tank 2 is provided with a liquid level meter 17, the pipeline I3 is provided with a regulating valve V18, and referring to fig. 2, the liquid level meter 17 is in control connection with the regulating valve V18.
Example 5
This example compares to examples 1-4 with the difference that the hydrogen line I6 is a 1.0MPa hydrogen line.
Example 6
This example compares with examples 1-4 with the difference that the hydrogen line II8 is a 2.4MPa hydrogen line.
Example 7
This embodiment further illustrates the scheme by taking a silicon tetrachloride conveying system of a cold hydrogenation section in a production apparatus for producing 15 ten thousand tons/year polysilicon.
This system specifically includes one-level buffer tank 1 and second grade buffer tank 2, refers to fig. 2, and one-level buffer tank 1 passes through pipeline I3 and connects second grade buffer tank 2, is equipped with delivery pump I4 on the pipeline I3, one-level buffer tank 1 is connected with silicon tetrachloride feed line 5, hydrogen pipeline I6 and exhaust pipe I7, be connected with hydrogen pipeline II8, exhaust pipe II9 and silicon tetrachloride discharge pipeline 10 on the second grade buffer tank 2, be equipped with delivery pump II19 on the silicon tetrachloride discharge pipeline 10.
In this embodiment, pressure gauge I11 is arranged on first-stage buffer tank 1, regulating valve I12 is arranged on exhaust pipe I7, regulating valve II13 is arranged on hydrogen pipeline I6, and pressure gauge I11 is respectively in control connection with regulating valve I12 and regulating valve II 13.
In this embodiment, be equipped with pressure gauge II14 on the second grade buffer tank 2, be equipped with governing valve III15 on the exhaust pipe II9, be equipped with governing valve IV16 on the hydrogen pipeline II8, pressure gauge II14 respectively with governing valve III15, governing valve IV16 control connection.
In this embodiment, the secondary buffer tank 2 is provided with a liquid level meter 17, the pipeline I3 is provided with an adjusting valve V18, and the liquid level meter 17 is connected with the adjusting valve V18 in a controlled manner.
In this embodiment, the hydrogen pipeline I6 is a 1.0MPa hydrogen pipeline; the hydrogen pipeline II8 is a 2.4MPa hydrogen pipeline.
When the system is used, silicon tetrachloride from a rectification section in a polycrystalline silicon production process enters a primary buffer tank 1, the pressure in the primary buffer tank 1 is regulated by the primary buffer tank 1 through a regulating valve I12 and a regulating valve II13 to keep stable, namely when the pressure in the primary buffer tank 1 is lower than a set value, the regulating valve II13 on a hydrogen pipeline I6 is opened, and 1.0MPa hydrogen is supplemented into the primary buffer tank 1; when the pressure of the first-stage buffer tank 1 is higher than a set value, the regulating valve I12 is opened, the first-stage buffer tank 1 discharges part of gas to a waste gas system, then silicon tetrachloride in the first-stage buffer tank 1 is pressurized to a first gradient through the delivery pump I4, the pressurized silicon tetrachloride is delivered to the second-stage buffer tank 2 through the pipeline I, and the amount of the silicon tetrachloride entering the second-stage buffer tank 2 is controlled through the liquid level meter 17 and the regulating valve V18 so as to ensure the stability of the liquid level of the second-stage buffer tank 2. In this embodiment, the pressure control range of the primary buffer tank 1 is 0.3 to 0.9mpa.
The pressure of the secondary buffer tank 2 is regulated by the secondary buffer tank 2 through a regulating valve III15 and a regulating valve IV16 to keep stable, namely when the pressure of the secondary buffer tank 2 is lower than a set value, the regulating valve IV16 on the hydrogen pipeline II8 is opened, 2.4MPa hydrogen is supplemented into the secondary buffer tank 2, when the pressure in the secondary buffer tank 2 is higher than the set value, the regulating valve III15 on the exhaust pipe II9 is opened, and the pressure in the secondary buffer tank 2 is discharged to an exhaust system through the exhaust pipe II 9; then the silicon tetrachloride in the secondary buffer tank 2 is pressurized by a delivery pump, and the silicon tetrachloride which reaches the expected pressure after secondary pressurization is delivered to the cold hydrogenation section. In this embodiment, the pressure control range of the secondary buffer tank 2 is 1.8 to 2.2MPa.
After the system is implemented, the total conveying capacity of the silicon tetrachloride of the production line is 1050m & lt 3 & gt/year, and if the traditional pressurizing and lifting scheme is adopted and the pressure at the pump inlet is 0.5MPa, the traditional shielding pump is adoptedThe manufacturing technology needs to arrange 15 pumps, 10 pumps are opened for 5 standby, and the flow rate of a single pump is 120 m 3 H, lift 230m, pump efficiency 55%, power 240kW.
And (3) accounting the cost of the traditional equipment: according to 15 pumps: 27 ten thousand by 15 =405 ten thousand yuan;
and (3) accounting the cost of the cable and the switch cabinet: the unit price of the switch cabinet is 8.1 ten thousand yuan, the unit price of the cable is 303 yuan/m, and the total is 300 m;
15 pumps: 15 + (8.1 +2 × 303 × 300 ÷ 10000) =394.2 ten thousand yuan;
annual operating cost accounting: 240kw 0.85 × 10 × 8000h × 0.4 yuan/degree ÷ 10000=652.8 ten thousand yuan.
If the two-stage pressurizing and lifting scheme is adopted, only 4 pumps are needed for every 1-stage delivery pump, 3 pumps are started for 1 standby, and the flow of a single pump is 360m 3 H, lift 118m, pump efficiency 75% and power 260KW.
The equipment cost accounting of the scheme is as follows: 8 pumps: 25 ten thousand/8 =200 ten thousand yuan, 2 buffer tanks (a primary buffer tank 1 and a secondary buffer tank 2) are added, and the auxiliary buffer tanks and the installation are as follows: 100 ten thousand 2=200 ten thousand yuan, the total of the equipment cost: 400 ten thousand yuan;
and (3) accounting the cost of the cable and the switch cabinet: according to the unit price of the switch cabinet of 8.1 ten thousand yuan, the unit price of the cable of 303 yuan/m, the total 300 m: 8 pumps: 8 + (8.1 +2 × 303 × 300 ÷ 10000) =210.2 ten thousand yuan;
annual operating cost accounting: 260kw × 0.85 × 6 × 8000h × 0.4 yuan/degree ÷ 10000=424.3 ten thousand yuan.
As can be seen from the comparison, the system adopting the scheme can save (405 + 394.2) - (400 + 210.2) =189 ten thousand yuan from investment; the running cost can be saved by 652.8-424.3=228.5 ten thousand yuan each year.
Claims (6)
1. A silicon tetrachloride conveying system is characterized in that: including one-level buffer tank (1) and second grade buffer tank (2), second grade buffer tank (2) are connected through pipeline I (3) in one-level buffer tank (1), are equipped with delivery pump I (4) on pipeline I (3), one-level buffer tank (1) is connected with silicon tetrachloride feed line (5), hydrogen pipeline I (6) and exhaust pipe I (7), be connected with hydrogen pipeline II (8), exhaust pipe II (9) and silicon tetrachloride emission pipeline (10) on second grade buffer tank (2), be equipped with delivery pump II (19) on silicon tetrachloride emission pipeline (10).
2. A silicon tetrachloride delivery system according to claim 1, wherein: be equipped with pressure gauge I (11) on one-level buffer tank (1), be equipped with governing valve I (12) on exhaust pipe I (7), be equipped with governing valve II (13) on hydrogen pipeline I (6), pressure gauge I (11) respectively with governing valve I (12), governing valve II (13) control connection.
3. A silicon tetrachloride delivery system according to claim 1, wherein: be equipped with pressure gauge II (14) on second grade buffer tank (2), be equipped with governing valve III (15) on exhaust pipe II (9), be equipped with governing valve IV (16) on hydrogen pipeline II (8), pressure gauge II (14) respectively with governing valve III (15), governing valve IV (16) control connection.
4. A silicon tetrachloride delivery system according to claim 1, wherein: the secondary buffer tank (2) is provided with a liquid level meter (17), the pipeline I (3) is provided with a regulating valve V (18), and the liquid level meter (17) is connected with the regulating valve V (18) in a control mode.
5. A silicon tetrachloride delivery system according to any one of claims 1 to 4, wherein: the hydrogen pipeline I (6) is a 1.0MPa hydrogen pipeline.
6. A silicon tetrachloride delivery system according to any one of claims 1 to 4, wherein: the hydrogen pipeline II (8) is a 2.4MPa hydrogen pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221734802.1U CN217894433U (en) | 2022-07-07 | 2022-07-07 | Silicon tetrachloride conveying system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221734802.1U CN217894433U (en) | 2022-07-07 | 2022-07-07 | Silicon tetrachloride conveying system |
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| Publication Number | Publication Date |
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| CN217894433U true CN217894433U (en) | 2022-11-25 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202221734802.1U Active CN217894433U (en) | 2022-07-07 | 2022-07-07 | Silicon tetrachloride conveying system |
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- 2022-07-07 CN CN202221734802.1U patent/CN217894433U/en active Active
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