CN212988122U - Heat energy recovery system suitable for cold hydrogenation technology - Google Patents
Heat energy recovery system suitable for cold hydrogenation technology Download PDFInfo
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- CN212988122U CN212988122U CN202021859901.3U CN202021859901U CN212988122U CN 212988122 U CN212988122 U CN 212988122U CN 202021859901 U CN202021859901 U CN 202021859901U CN 212988122 U CN212988122 U CN 212988122U
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Abstract
The utility model discloses a heat recovery system suitable for in cold hydrogenation technology belongs to polycrystalline silicon production technical field, including scrubbing tower, heat exchanger and cooling unit, the scrubbing tower upper end is provided with gas outlet, be provided with air inlet I, gas outlet I and liquid outlet I on the heat exchanger, last air inlet II, gas outlet II and the liquid outlet II of being provided with of cooling unit, gas outlet is connected with air inlet I, gas outlet I is connected with air inlet II, has solved in the current cold hydrogenation technology, and heat recovery system is incomplete, leads to the extravagant problem of the energy to reduction in production cost.
Description
Technical Field
The utility model belongs to the technical field of polycrystalline silicon production, a cold hydrogenation system in polycrystalline silicon production is related to, concretely relates to heat recovery system suitable for in cold hydrogenation technology.
Background
In the technical field of polysilicon production, compared with the hot hydrogenation process, the cold hydrogenation process adopts a common fluidized bed reaction and has power consumptionLow and high STC conversion rate. The reaction principle of cold hydrogenation is: si +3SiCl4+H2=4SiHCl3. At present, in a cold hydrogenation process for producing polycrystalline silicon, process gas (hydrogen, trichlorosilane and a small amount of silicon-containing high-boiling-point substances) coming out from the top of a washing tower needs to be cooled to obtain a crude trichlorosilane product, and then the crude trichlorosilane product is sent to a rectification section for further treatment.
The existing process usually adopts a mode of combining a Freon cooling device or a circulating water cooling device with the Freon cooling device to cool the process gas to-30 ℃, and the gaseous hydrogen is discharged, so that the liquid trichlorosilane and a small amount of crude trichlorosilane product containing silicon high-boiling-point substances can be obtained.
In the daily production process of the cold hydrogenation system, the process gas coming out of the top of the washing tower needs to be cooled from 145 ℃ to-30 ℃ step by step to obtain a crude trichlorosilane product. The hydrogen and silicon tetrachloride raw materials need to be heated to 180 ℃ from 50 ℃ step by step before entering the vaporizer, and the heat load released by the process gas from the top of the washing tower when the temperature is reduced from 145 ℃ to 40 ℃ is about 6946KW by detecting the temperature of the tube side and the shell side of the existing heat exchanger, while the part of the heat load recovered by the hydrogen and silicon tetrachloride raw materials before entering the vaporizer is only 2214KW, the proportion is only 31.87%, and a large amount of heat is wasted.
For the above reasons, further optimization of the existing cold hydrogenation process and equipment is needed to reduce the waste of heat and save the production cost.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving the heat recovery system among the cold hydrogenation technology of prior art incomplete, lead to the energy extravagant, problem that manufacturing cost is higher.
In order to achieve the above purpose, the technical solution of the present invention is as follows:
the utility model provides a heat recovery system suitable for in cold hydrogenation technology, includes scrubbing tower, heat exchanger and cooling unit, the scrubbing tower upper end is provided with gas outlet, be provided with air inlet I, gas outlet I and liquid outlet I on the heat exchanger, last air inlet II, gas outlet II and the liquid outlet II of being provided with of cooling unit, gas outlet is connected with air inlet I, gas outlet I is connected with air inlet II.
Further, the heat energy recovery system suitable for the cold hydrogenation process further comprises a condensate collecting tank, wherein the condensate collecting tank is respectively connected with the liquid outlet I and the liquid outlet II and is used for storing condensate discharged from the liquid outlet I and the liquid outlet II.
Further, the cooling unit includes circulating water cooling device and freon cooling device, circulating water cooling device includes circulating water cooling air inlet, circulating water cooling gas outlet and liquid outlet I, freon cooling device includes freon cooling air inlet, freon cooling gas outlet and sets up the liquid outlet II in freon cooling device lower part, circulating water cooling air inlet is connected with gas outlet I, the circulating water cooling gas outlet is connected with freon cooling air inlet, liquid outlet I and liquid outlet II all are connected with the condensate holding tank.
Furthermore, the washing tower also comprises a washing tower air inlet arranged in the middle of the washing tower, a spraying liquid inlet arranged in the middle upper part of the washing tower and a slurry outlet arranged at the bottom of the washing tower.
Further, the heat exchanger is a phase change heat exchanger.
The utility model has the advantages that:
firstly, the utility model discloses in, between scrubbing tower and the cooling unit in the cold hydrogenation technology of current, add the heat exchanger, it is incomplete to have solved the heat recovery system among the cold hydrogenation technology of prior art, leads to the energy extravagant, the higher problem of manufacturing cost.
Secondly, in the utility model discloses in, this heat recovery system suitable for in cold hydrogenation technology still includes the condensate holding vessel, the condensate holding vessel is used for collecting, stores liquid outlet I and liquid outlet II exhaust condensate-crude trichlorosilane product, the temperature in the centralized control condensate holding vessel of being convenient for.
Thirdly, the utility model discloses in, the cooling unit includes circulating water cooling device and freon cooling device, perhaps according to the actual production condition, can increase multistage circulating water cooling device, increases multistage freon cooling device even to reach the process gas that comes out the scrubbing tower top and cool off to-30 ℃'s purpose from 145 ℃ step by step.
Fourthly, in the utility model, the washing tower also comprises a washing tower air inlet arranged in the middle of the washing tower, the washing tower air inlet is connected with a bubbling tank at the front end, and the gas treated in the bubbling tank is introduced into the washing tower through the washing tower air inlet; and (3) spraying and cooling the gas in the washing tower by the spraying liquid entering from the spraying liquid inlet, and discharging most of high-boiling-point substances from a slag slurry outlet at the bottom of the washing tower.
Fifthly, the utility model discloses in, the heat exchanger adopts phase transition heat exchanger, is suitable for this workshop section to the little special demand of temperature difference change.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural view of embodiment 2.
Fig. 3 is a schematic diagram of the connections of the main heat exchangers in the cold hydrogenation process.
Wherein, 1, a washing tower; 2. a heat exchanger; 3. a cooling unit; 4. a condensate collection tank; 5. a circulating water cooling device; 6. a freon cooling device; 11. a gas outlet; 12. a scrubber gas inlet; 13. a spray liquid inlet; 14. a slurry outlet; 21. an air inlet I; 22. an air outlet I; 23. a liquid outlet I; 31. an air inlet II; 32. an air outlet II; 33. a liquid outlet II; 51. a circulating water cooling air inlet; 52. a circulating water cooling air outlet; 53. a liquid outlet I; 61. a freon cooling air inlet; 62. a Freon cooling gas outlet; 63. and a liquid outlet 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
Referring to fig. 1, a heat energy recovery system suitable for cold hydrogenation technology belongs to polycrystalline silicon production technical field, including scrubbing tower 1, heat exchanger 2 and cooling unit 3, scrubbing tower 1 upper end is provided with gas outlet 11, be provided with air inlet I21, gas outlet I22 and liquid outlet I23 on the heat exchanger 2, be provided with air inlet II31, gas outlet II32 and liquid outlet II33 on the cooling unit 3, gas outlet 11 is connected with air inlet I21, gas outlet I22 is connected with air inlet II 31.
The embodiment is the most basic implementation manner, the heat exchanger 2 is additionally arranged, so that the problem of energy waste caused by incomplete heat energy recovery system in the cold hydrogenation process in the prior art can be solved, and the heat recycling rate can be obviously improved.
Example 2
Referring to fig. 2 and 3, a heat energy recovery system suitable for a cold hydrogenation process belongs to the technical field of polysilicon production, and comprises a washing tower 1, a heat exchanger 2 and a cooling unit 3, wherein a gas outlet 11 is arranged at the upper end of the washing tower 1, a gas inlet I21, a gas outlet I22 and a liquid outlet I23 are arranged on the heat exchanger 2, a gas inlet II31, a gas outlet II32 and a liquid outlet II33 are arranged on the cooling unit 3, the gas outlet 11 is connected with a gas inlet I21, and the gas outlet I22 is connected with a gas inlet II 31.
Preferably, the heat energy recovery system suitable for the cold hydrogenation process further comprises a condensate collecting tank 4, wherein the condensate collecting tank 4 is respectively connected with the liquid outlet I23 and the liquid outlet II33 and is used for storing condensate discharged from the liquid outlet I23 and the liquid outlet II 33.
Preferably, cooling unit 3 includes circulating water cooling device 5 and freon cooling device 6, circulating water cooling device 5 includes circulating water cooling air inlet 51, circulating water cooling gas outlet 52 and liquid outlet I53, freon cooling device 6 includes freon cooling air inlet 61, freon cooling gas outlet 62 and sets up liquid outlet II63 in freon cooling device lower part, circulating water cooling air inlet 51 is connected with gas outlet I22, circulating water cooling gas outlet 52 is connected with freon cooling air inlet 61, liquid outlet I23, liquid outlet I53 and liquid outlet II63 all are connected with condensate collection tank 4.
Preferably, the washing tower 1 further comprises a washing tower gas inlet 12 arranged in the middle of the washing tower 1, a spray liquid inlet 13 arranged in the middle upper part of the washing tower 1, and a slurry outlet 14 arranged at the bottom of the washing tower 1.
Preferably, the heat exchanger 2 is a phase change heat exchanger 2.
By adopting the technical scheme of this embodiment, with reference to fig. 3, the heat load after heat exchange of other heat exchangers when the phase change heat exchanger in the technical scheme is not provided in the prior art is counted, as shown in table 1.
TABLE 1
Table 2 shows the heat load of the adjacent phase change heat exchangers after adding a new phase change heat exchanger, and the temperature statistics are shown in table 2.
TABLE 2
As can be seen from tables 1 and 2, after the step heat exchange of the technical scheme is adopted, the recovered heat is promoted to 3689KW from the previous 2214KW, and the released heat is promoted to 57.43% from the previous 31.87%. The hydrogen preheater and the silicon tetrachloride preheater are heated by adopting steam, the hydrogen preheater and the silicon tetrachloride preheater can be temporarily stopped after the newly-added heat exchanger is used, the steam is saved by about 2.5t/h, and each ton of steam is calculated according to 150 yuan, namely 1200 ten thousand yuan/year can be saved by 4 cold hydrogenation production lines. The tube pass operating pressure of the newly added heat exchanger, namely the phase change heat exchanger, is 2.6Mpa, and the shell pass operating pressure is 3.0 Mpa.
Claims (5)
1. A heat energy recovery system suitable for cold hydrogenation technology which characterized in that: including scrubbing tower (1), heat exchanger (2) and cooling unit (3), scrubbing tower (1) upper end is provided with gas outlet (11), be provided with air inlet I (21), gas outlet I (22) and liquid outlet I (23) on heat exchanger (2), be provided with air inlet II (31), gas outlet II (32) and liquid outlet II (33) on cooling unit (3), gas outlet (11) are connected with air inlet I (21), gas outlet I (22) are connected with air inlet II (31).
2. A heat energy recovery system suitable for use in a cold hydrogenation process according to claim 1, wherein: the device is characterized by further comprising a condensate collecting tank (4), wherein the condensate collecting tank (4) is respectively connected with the liquid outlet I (23) and the liquid outlet II (33) and is used for storing condensate discharged from the liquid outlet I (23) and the liquid outlet II (33).
3. A heat energy recovery system suitable for use in a cold hydrogenation process according to claim 2, wherein: cooling unit (3) include circulating water cooling device (5) and freon cooling device (6), circulating water cooling device (5) are including circulating water cooling air inlet (51), circulating water cooling gas outlet (52) and liquid outlet I (53), freon cooling device (6) are including freon cooling air inlet (61), freon cooling gas outlet (62) and set up liquid outlet II (63) in freon cooling device lower part, circulating water cooling air inlet (51) are connected with gas outlet I (22), circulating water cooling gas outlet (52) are connected with freon cooling air inlet (61), liquid outlet I (23), liquid outlet I (53) and liquid outlet II (63) all are connected with condensate collection tank (4).
4. A heat energy recovery system suitable for use in a cold hydrogenation process according to claim 3, wherein: the washing tower (1) further comprises a washing tower air inlet (12) arranged in the middle of the washing tower (1), a spraying liquid inlet (13) arranged at the middle upper part of the washing tower (1), and a slurry outlet (14) arranged at the bottom of the washing tower (1).
5. A heat energy recovery system suitable for use in a cold hydrogenation process according to claim 4, wherein: the heat exchanger (2) is a phase change heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021859901.3U CN212988122U (en) | 2020-08-31 | 2020-08-31 | Heat energy recovery system suitable for cold hydrogenation technology |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113387364A (en) * | 2021-05-08 | 2021-09-14 | 内蒙古新特硅材料有限公司 | Method and system for treating cold hydrogenation synthesis gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113387364A (en) * | 2021-05-08 | 2021-09-14 | 内蒙古新特硅材料有限公司 | Method and system for treating cold hydrogenation synthesis gas |
| CN113387364B (en) * | 2021-05-08 | 2023-02-28 | 内蒙古新特硅材料有限公司 | Method and system for treating cold hydrogenation synthesis gas |
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Assignee: Sichuan Yongxiang Energy Technology Co.,Ltd. Assignor: SICHUAN YONGXIANG NEW ENERGY Co.,Ltd. Contract record no.: X2023510000014 Denomination of utility model: A Heat Recovery System Suitable for Cold Hydrogenation Process Granted publication date: 20210416 License type: Common License Record date: 20230816 |