CN219848193U - Slag discharging system of cold hydrogenation crude distillation column - Google Patents
Slag discharging system of cold hydrogenation crude distillation column Download PDFInfo
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- CN219848193U CN219848193U CN202321258353.2U CN202321258353U CN219848193U CN 219848193 U CN219848193 U CN 219848193U CN 202321258353 U CN202321258353 U CN 202321258353U CN 219848193 U CN219848193 U CN 219848193U
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- tower
- slag
- crude distillation
- crude
- distillation column
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- 239000002893 slag Substances 0.000 title claims abstract description 107
- 238000004821 distillation Methods 0.000 title claims abstract description 89
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 28
- 238000007599 discharging Methods 0.000 title claims abstract description 27
- 238000005406 washing Methods 0.000 claims abstract description 72
- 239000002002 slurry Substances 0.000 claims abstract description 50
- 239000000463 material Substances 0.000 claims abstract description 21
- 230000005587 bubbling Effects 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 229910021420 polycrystalline silicon Inorganic materials 0.000 abstract description 4
- 229920005591 polysilicon Polymers 0.000 abstract description 4
- 238000009835 boiling Methods 0.000 description 12
- 239000005046 Chlorosilane Substances 0.000 description 10
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 10
- 239000007788 liquid Substances 0.000 description 10
- 229910001510 metal chloride Inorganic materials 0.000 description 7
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 239000005049 silicon tetrachloride Substances 0.000 description 6
- 238000003786 synthesis reaction Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 4
- 239000005052 trichlorosilane Substances 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 239000011863 silicon-based powder Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- FAIAAWCVCHQXDN-UHFFFAOYSA-N phosphorus trichloride Chemical compound ClP(Cl)Cl FAIAAWCVCHQXDN-UHFFFAOYSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- FAQYAMRNWDIXMY-UHFFFAOYSA-N trichloroborane Chemical compound ClB(Cl)Cl FAQYAMRNWDIXMY-UHFFFAOYSA-N 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229920000548 poly(silane) polymer Polymers 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
Abstract
The utility model discloses a slag discharging system of a cold hydrogenation crude distillation column, which belongs to the technical field of polysilicon production and comprises a washing column for collecting outlet materials of a cold hydrogenation reactor and a crude distillation column for collecting cold hydrogenation synthetic condensate materials, wherein a pump for conveying slag discharged from the crude distillation column to a tower kettle of the washing column is arranged between the crude distillation column and the washing column, and the washing column is connected with a slag slurry device for collecting slag materials of the washing column. According to the utility model, the tower bottom pump of the crude distillation tower is arranged between the crude distillation tower and the washing tower, and the slag of the crude distillation tower is conveyed to the washing tower by the tower bottom pump of the crude distillation tower, so that continuous slag discharge of the crude distillation tower can be realized, the problem of pipeline blockage caused by intermittent slag discharge of the crude distillation tower is solved, meanwhile, the synthetic slag discharge amount is reduced, the slag slurry load is reduced, and the stable operation of the crude distillation tower is ensured.
Description
Technical Field
The utility model relates to the technical field of polysilicon production, in particular to a slag discharging system of a cold hydrogenation crude distillation column.
Background
In the production process of polysilicon, the processing method, processing load and whether the slag slurry can be continuously received by the slag slurry device are all the restriction factors influencing the stable operation of polysilicon cold hydrogenation synthesis.
In the prior art production, slag is discharged from a cold hydrogenation synthetic washing tower and a crude distillation tower through independent slag discharge pipelines to a slag slurry device, and the slag slurry device is used for further treatment and recovery (shown in figure 1 of the specification). Because the washing tower and the crude distillation tower respectively use independent slag discharging pipelines, the chlorosilane material amount discharged to the slag slurry device is increased, the load of the slag slurry device is large, and the construction cost and the slag slurry treatment cost of the slag slurry device are increased.
In addition, the existing deslagging process adopts intermittent operation, because the pressure of the crude distillation column is relatively low, slag materials such as metal chloride and high boiling point are contained in the slag materials at the bottom of the crude distillation column, along with long-time intermittent operation, the metal chloride is attached to the inner wall of a deslagging pipeline, so that the deslagging pipeline is blocked for a long time, high boiling aggregation at the bottom of the crude distillation column is finally caused, the temperature of the column bottom is increased, the consumption of heat source steam is increased, the production cost is increased, and meanwhile, the product quality of the crude distillation column is influenced.
Related content related to trichlorosilane production technology in the prior patent literature, for example, chinese patent publication No. CN106554019B discloses a trichlorosilane synthesis tail gas purification system, which comprises a washing tower and a crude distillation tower, wherein the washing tower is used for leaching synthesis tail gas through chlorosilane washing liquid, silicon powder and part of high boiling point components in the synthesis tail gas are output to a raffinate absorption system along with the chlorosilane washing liquid from a liquid outlet of the washing tower, and low boiling point components, the rest of high boiling point components and low boiling point components in the chlorosilane washing liquid are output to the crude distillation tower as primarily purified synthesis tail gas from a gas phase outlet of the washing tower; the crude distillation tower is used for leaching the primarily purified synthetic tail gas through the chlorosilane washing liquid, the rest high boiling components in the primarily purified synthetic tail gas are output to a waste chlorosilane storage tank along with the chlorosilane washing liquid from a liquid outlet of the crude distillation tower, and the primarily purified synthetic tail gas and the low boiling components in the chlorosilane washing liquid are output to a chlorosilane cooling and purifying system from a gas phase outlet of the crude distillation tower. In the scheme, high boiling point components in the crude distillation column are output to a waste chlorosilane storage tank through a extraction pipeline at the bottom of the crude distillation column, and high boiling point components in the washing column are output to a residual liquid absorption system through a residual liquid discharge pipeline at the bottom of the washing column.
Therefore, how to process and recover the slag slurry normally while avoiding the blockage of the pipeline is a technical problem facing the person skilled in the art.
Disclosure of Invention
The utility model aims to provide a slag discharging system of a cold hydrogenation crude distillation column, which solves the problems in the prior art, and the slag discharging system can realize continuous slag discharging of the crude distillation column, eliminate the problem of pipeline blockage caused by intermittent slag discharging of the crude distillation column, reduce the synthetic slag discharging amount, reduce the slag slurry load and ensure the stable operation of the crude distillation column by arranging a pump of a tower kettle of the crude distillation column between the crude distillation column and a washing column and utilizing the pump of the tower kettle of the crude distillation column to convey slag discharging of the crude distillation column to the washing column.
In order to achieve the above object, the present utility model provides the following solutions:
the utility model provides a slag discharging system of a cold hydrogenation crude distillation column, which comprises a washing column for collecting outlet materials of a cold hydrogenation reactor and a crude distillation column for collecting cold hydrogenation synthetic condensate materials, wherein a pump for conveying slag discharged from the crude distillation column to a tower kettle of the washing column is arranged between the crude distillation column and the washing column, and the washing column is connected with a slag slurry device for collecting slag materials of the washing column.
Preferably, the slurry device comprises a slurry receiving tank.
Preferably, the slurry receiving tank is connected to a dryer or a rotary drum filter.
Preferably, the top of the slurry receiving tank is connected with the washing tower, and the bottom of the slurry receiving tank is connected with the dryer or the rotary drum filter.
Preferably, the scrubber operating pressure is 2.5mpa, the operating temperature is 145 ℃, the crude distillation column operating pressure is 0.2mpa, and the operating temperature is 110 ℃.
Preferably, a bubbling device is arranged in the washing tower.
Preferably, the outlet of the bottom pump of the crude distillation column is connected with a branch leading to the crude distillation column.
Preferably, a flow regulating valve is arranged on the branch.
Compared with the prior art, the utility model has the following technical effects:
(1) According to the utility model, the tower bottom pump of the crude distillation tower is arranged between the crude distillation tower and the washing tower, and the slag of the crude distillation tower is conveyed to the washing tower by the tower bottom pump of the crude distillation tower, so that continuous slag discharge of the crude distillation tower can be realized, the problem of pipeline blockage caused by intermittent slag discharge of the crude distillation tower is solved, meanwhile, the synthetic slag discharge amount is reduced, the slag slurry load is reduced, and the stable operation of the crude distillation tower is ensured;
(2) The utility model conveys the slag discharged by the washing tower to the slurry receiving tank, temporarily stores the slag in the slurry receiving tank, and then carries out further treatment and recovery through the dryer or the rotary drum filter, so that the slag discharged by the washing tower can be ready to be received by the slurry receiving tank at any time, and the stable operation of the system is ensured;
(3) The utility model connects with the branch leading to the crude tower at the outlet of the crude tower bottom pump, can carry on the crude distillation process again to the slag material reflux discharged by the crude tower, in addition, set up the flow control valve on the branch, can regulate the slag material that returns to the crude tower by the flow control valve, regulate the slag material amount entering the scrubber at the same time.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present utility model, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a slag discharging system used in the prior art;
FIG. 2 is a schematic diagram of a slag discharging system according to the present utility model;
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The utility model aims to provide a slag discharging system of a cold hydrogenation crude distillation column, which solves the problems in the prior art, and by arranging a crude distillation column bottom pump between the crude distillation column and a washing column, slag discharged from the crude distillation column is conveyed to the washing column by using the crude distillation column bottom pump, so that continuous slag discharge of the crude distillation column can be realized, the problem of pipeline blockage caused by intermittent slag discharge of the crude distillation column is solved, meanwhile, the synthetic slag discharge amount is reduced, the slag slurry load is reduced, and the stable operation of the crude distillation column is ensured.
In order that the above-recited objects, features and advantages of the present utility model will become more readily apparent, a more particular description of the utility model will be rendered by reference to the appended drawings and appended detailed description.
As shown in FIG. 2, the present utility model provides a slag discharging system of a cold hydrogenation crude distillation column, comprising a washing column for collecting the outlet material of a cold hydrogenation reactor and a crude distillation column for collecting the condensed material of the cold hydrogenation synthesis. The crude tower is communicated with the washing tower through a pipeline, and a crude tower kettle pump is arranged on the pipeline, and can convey slag of the crude tower to the washing tower, so that the method that slag is discharged to a slag-slurry device through respective independent slag discharging pipelines in the crude tower and the washing tower in the prior art is changed, and the washing tower mainly recovers silicon tetrachloride in slag discharging components of the crude tower for slag discharging of the entering crude tower. The washing tower is connected with a slag-slurry device for collecting slag of the washing tower, the slag discharged from the coarse distillation tower can be conveyed to the washing tower through a pump at the bottom of the coarse distillation tower, and is discharged to the slag-slurry device together with the slag of the washing tower, and further recovery treatment is carried out on the slag through the slag-slurry device. In the technical scheme of the utility model, the main components of the residue discharge of the crude tower in a specific embodiment are as follows: 97.48% of silicon tetrachloride, 2.52% of boron trichloride and 2000kg/h of slag discharge. The main components of the slag discharged by the washing tower are as follows: 73.3% of silicon tetrachloride, 15.8% of trichlorosilane, 3.0% of silicon powder, 5% of metal chloride, 2.4% of phosphorus trichloride, 0.01% of polysilane and 3000kg/h of slag discharge. The slag slurry treatment is mainly as follows: silicon powder, metal chloride, phosphorus trichloride and boron trichloride, and the consumption of chloride ions is reduced by recycling silicon tetrachloride and trichlorosilane. The chloride ions are mainly provided by the silicon tetrachloride in the cold hydrogenation production process, and the deslagging mode can reduce the discharge of the silicon tetrachloride from the source. In summary, the utility model can realize continuous deslagging of the crude distillation column by arranging the crude distillation column bottom pump between the crude distillation column and the washing column and conveying deslagging of the crude distillation column to the washing column by utilizing the crude distillation column bottom pump, thereby eliminating the problem of pipeline blockage caused by intermittent deslagging of the crude distillation column, reducing the synthetic deslagging amount, reducing the slag slurry load and ensuring the stable operation of the crude distillation column.
It should be noted that: the existing deslagging mode adopts intermittent operation, because the pressure of the crude distillation column is relatively low, slag materials such as metal chloride and high boiling point are contained in the slag materials at the bottom of the crude distillation column, along with long-time intermittent operation, the metal chloride is adhered to the inner wall of a deslagging pipeline, so that the deslagging pipeline is blocked for a long time, high boiling aggregation at the bottom of the crude distillation column is finally caused, the temperature of the column bottom is increased, the consumption of heat source steam is increased, the production cost is increased, and meanwhile, the product quality of the crude distillation column is influenced. The utility model changes the prior intermittent operation mode by arranging the tower bottom pump of the crude tower to be connected with the washing tower, can realize continuous slag discharge of the crude tower, further solves the problem of adhesion of metal chloride, and avoids blockage of a slag discharge pipeline. Meanwhile, the slag of the coarse distillation tower is not directly discharged to the slag-slurry device, but is discharged to the slag-slurry device together with the slag of the washing tower after being treated by the washing tower, and part of the slag is treated in the process, so that the synthetic slag discharge amount of cold hydrogenation synthetic condensate is reduced, and the slag-slurry load is reduced.
The slag-slurry device comprises a slurry receiving tank, slag discharged from the washing tower can be temporarily stored in a slurry collecting tank for subsequent treatment, or the slurry collecting tank is connected with a recovery treatment device, the recovery treatment device is utilized to directly treat the slag in the slurry collecting tank, the slag discharged from the washing tower can be prepared to be received by the slurry receiving tank at any time, and the stable operation of the system is ensured.
The recovery processing device connected with the slurry receiving tank can be a dryer or a rotary drum filter, and the slag discharged from the washing tower is dehydrated through the dryer or the rotary drum filter and then is further processed and recovered.
The top of the slurry receiving tank is connected with the washing tower, and the bottom of the slurry receiving tank is connected with the dryer or the rotary drum filter, so that the slurry receiving tank can be arranged according to the flowing direction of the slag, and the gravity of the slag can be utilized to promote the flow of the slag to the direction of the dryer or the rotary drum filter.
The operating pressure of the scrubber was 2.5mpa, the operating temperature was 145 c, the operating pressure of the crude distillation column was 0.2mpa, and the operating temperature was 110 c. The washing tower belongs to a high-pressure tower, the crude tower belongs to a low-pressure tower, and slag in the crude tower is conveyed to the washing tower after being pressurized by a tower kettle pump of the crude tower.
The bubbling device is arranged in the washing tower, bubbling is carried out through the bubbling device, and the bubbling device is used for improving the deslagging concentration of the washing tower. The slag material directly discharged to the slag slurry device in the crude distillation column is conveyed to the washing column through a pump at the bottom of the crude distillation column, is mixed with the slag slurry of the washing column after bubbling in the washing column, and is discharged to a slag material receiving tank through a slag discharge pipeline of the washing column. The problem of blockage of the slag discharge pipeline of the crude distillation column is limited avoided, and the purpose of continuous slag discharge of the crude distillation column is achieved.
The outlet of the tower bottom pump of the crude tower is connected with a branch leading to the crude tower, and the residue reflux discharged from the crude tower can be subjected to a secondary crude distillation process.
In addition, a flow regulating valve is arranged on the branch, and the slag quantity returned to the crude tower can be regulated by the flow regulating valve, and the slag quantity entering the washing tower can be regulated.
The principles and embodiments of the present utility model have been described in detail with reference to specific examples, which are provided to facilitate understanding of the method and core ideas of the present utility model; also, it is within the scope of the present utility model to be modified by those of ordinary skill in the art in light of the present teachings. In view of the foregoing, this description should not be construed as limiting the utility model.
Claims (8)
1. A slag discharging system of a cold hydrogenation crude distillation column is characterized in that: the device comprises a washing tower for collecting outlet materials of a cold hydrogenation reactor and a crude tower for collecting cold hydrogenation synthetic condensate materials, wherein a crude tower kettle pump for conveying slag discharged from the crude tower to the washing tower is arranged between the crude tower and the washing tower, and the washing tower is connected with a slag slurry device for collecting slag materials of the washing tower.
2. The cold hydrogenation crude distillation column slag discharging system according to claim 1, wherein: the slurry device includes a slurry receiving tank.
3. The cold hydrogenation crude distillation column slag discharging system according to claim 2, wherein: the slurry receiving tank is connected with a dryer or a rotary drum filter.
4. The cold hydrogenation crude distillation column slag discharging system according to claim 3, wherein: the top of the slurry receiving tank is connected with the washing tower, and the bottom of the slurry receiving tank is connected with the dryer or the rotary drum filter.
5. The cold hydrogenation crude distillation column slag discharging system according to claim 1, wherein: the operating pressure of the washing tower is 2.5mpa, the operating temperature is 145 ℃, the operating pressure of the crude distillation tower is 0.2mpa, and the operating temperature is 110 ℃.
6. The cold hydrogenation crude distillation column slag discharging system according to claim 1, wherein: a bubbling device is arranged in the washing tower.
7. The cold hydrogenation crude distillation column slag discharging system according to claim 1, wherein: the outlet of the tower bottom pump of the crude tower is connected with a branch leading to the crude tower.
8. The cold hydrogenation crude distillation column slag discharging system according to claim 7, wherein: and the branch is provided with a flow regulating valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321258353.2U CN219848193U (en) | 2023-05-23 | 2023-05-23 | Slag discharging system of cold hydrogenation crude distillation column |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321258353.2U CN219848193U (en) | 2023-05-23 | 2023-05-23 | Slag discharging system of cold hydrogenation crude distillation column |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219848193U true CN219848193U (en) | 2023-10-20 |
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| CN202321258353.2U Active CN219848193U (en) | 2023-05-23 | 2023-05-23 | Slag discharging system of cold hydrogenation crude distillation column |
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| Country | Link |
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| CN (1) | CN219848193U (en) |
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2023
- 2023-05-23 CN CN202321258353.2U patent/CN219848193U/en active Active
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