CN221191574U - Synthetic material gas desorption separator - Google Patents
Synthetic material gas desorption separator Download PDFInfo
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- CN221191574U CN221191574U CN202323089720.3U CN202323089720U CN221191574U CN 221191574 U CN221191574 U CN 221191574U CN 202323089720 U CN202323089720 U CN 202323089720U CN 221191574 U CN221191574 U CN 221191574U
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- buffer tank
- pipe
- space
- liquid level
- synthesis gas
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- 229920002994 synthetic fiber Polymers 0.000 title claims abstract description 27
- 238000003795 desorption Methods 0.000 title abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 238000009826 distribution Methods 0.000 claims abstract description 27
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 18
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 239000003507 refrigerant Substances 0.000 claims abstract description 7
- 238000002955 isolation Methods 0.000 claims abstract 2
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 238000010926 purge Methods 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 abstract description 20
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 20
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 17
- 239000007789 gas Substances 0.000 abstract description 15
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 229910021420 polycrystalline silicon Inorganic materials 0.000 abstract description 3
- 229920005591 polysilicon Polymers 0.000 abstract description 2
- 239000005046 Chlorosilane Substances 0.000 description 15
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 15
- 239000012530 fluid Substances 0.000 description 13
- 238000005984 hydrogenation reaction Methods 0.000 description 7
- 239000000463 material Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 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 2
- 230000000694 effects Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000005049 silicon tetrachloride Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- MROCJMGDEKINLD-UHFFFAOYSA-N dichlorosilane Chemical compound Cl[SiH2]Cl MROCJMGDEKINLD-UHFFFAOYSA-N 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000011863 silicon-based powder Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 1
- 239000005052 trichlorosilane Substances 0.000 description 1
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- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model discloses a synthetic material gas desorption separation device, relates to the technical field of polysilicon production, and mainly aims to desorb and recycle hydrogen in cold hydrogenated synthetic material before rectification. The main technical scheme of the utility model is as follows: a synthesis gas desorption separation device comprising: the lower end of the buffer tank is connected with one end of a conveying pipe, and the other end of the conveying pipe is connected with the rectifying tower; the synthetic material conveying pipe penetrates through the top wall of the buffer tank and is connected with the distribution pipe, the distribution pipe is arranged above the liquid level of the buffer tank, and a plurality of through holes are uniformly distributed on the pipe wall of the distribution pipe; the condenser includes first space and the second space of mutual isolation, and first space is used for supplying the refrigerant to flow, and the upper end in second space is connected in the one end of recovery pipe and buffer tube's one end respectively, and the other end in buffer tube connects in the upper end of buffer tank, and the lower extreme in second space is connected in the one end of back flow, and the roof of buffer tank is run through to the other end of back flow to extend to below the liquid level of buffer tank.
Description
Technical Field
The utility model relates to the technical field of polysilicon production, in particular to a synthesis gas desorption separation device.
Background
In the process of producing polycrystalline silicon by an improved Siemens method, synthetic materials of a cold hydrogenation working section are synthesized by silicon powder, silicon tetrachloride and hydrogen under the conditions of high temperature and high pressure, a large amount of hydrogen is dissolved in the synthetic materials under the conditions of high pressure, and the synthetic materials are directly sent to a rectifying tower to separate silicon tetrachloride, trichlorosilane, dichlorosilane and other components.
Disclosure of utility model
In view of this, the present utility model provides a synthesis gas desorption separation device, which is mainly aimed at desorbing and recovering hydrogen in cold hydrogenated synthesis material before rectifying the same.
In order to achieve the above purpose, the present utility model mainly provides the following technical solutions:
The utility model provides a synthesis gas desorption separation device, which comprises: buffer tank, synthetic material conveying pipe and condenser;
The lower end of the buffer tank is connected with one end of a conveying pipe, and the other end of the conveying pipe is connected with the rectifying tower;
The synthetic material conveying pipe penetrates through the top wall of the buffer tank and is connected with the distribution pipe, the distribution pipe is arranged above the liquid level of the buffer tank, and a plurality of through holes are uniformly distributed on the pipe wall of the distribution pipe;
the condenser comprises a first space and a second space which are isolated from each other, wherein the first space is used for supplying refrigerant to flow, the upper end of the second space is respectively connected with one end of a recovery pipe and one end of a buffer pipe, the other end of the buffer pipe is connected with the upper end of the buffer tank, the lower end of the second space is connected with one end of a return pipe, and the other end of the return pipe penetrates through the top wall of the buffer tank and extends below the liquid level of the buffer tank.
The aim and the technical problems of the utility model can be further realized by adopting the following technical measures.
Optionally, the distribution pipe is annular, the distribution pipe level set up in the buffer tank.
Optionally, the condenser is a horizontal tubular heat exchanger, the first space is a tube side of the tubular heat exchanger, and the second space is a shell side of the tubular heat exchanger.
Optionally, the system further comprises a pressure sensor and a pressure regulating valve, wherein the pressure sensor is installed at the upper end of the buffer tank, the pressure regulating valve is installed in the recovery pipe, and the pressure sensor and the pressure regulating valve are integrated in the DCS control system.
Optionally, the device further comprises a liquid level sensor and a liquid level regulating valve, wherein the liquid level sensor is installed in the buffer tank, the liquid level regulating valve is installed in the conveying pipe, and the liquid level sensor and the liquid level regulating valve are integrated in the DCS control system.
Optionally, the buffer tank further comprises a purge pipe connected to the upper end of the buffer tank.
Optionally, a control valve is further included, and the control valve is mounted to the purge tube.
Optionally, the buffer tank adopts a spherical kettle.
By means of the technical scheme, the utility model has at least the following advantages:
The cold hydrogenation synthetic material is conveyed to the buffer tank through the synthetic material conveying pipe, sprayed out to the gas phase space of the buffer tank in a mist form through a plurality of through holes of the distribution pipe, so that the synthetic material liquid is favorable for dispersing drops of the synthetic material, the desorption of hydrogen in the synthetic material is facilitated, gas phase fluid in the buffer tank is conveyed to the second space of the condenser through the buffer pipe, chlorosilane in the gas phase fluid is condensed under the action of a refrigerant, and returned to the buffer tank through the return pipe, and the gas-liquid separation of hydrogen and chlorosilane in the synthetic material is realized.
Moreover, because the other end of the return pipe extends below the liquid level of the buffer tank, gas phase fluid in the buffer tank is prevented from entering the return pipe, so that the buffer tank, the buffer pipe, the condenser and the return pipe form a chlorosilane condensation recovery passage, and the separation efficiency of hydrogen and chlorosilane is improved.
Drawings
Fig. 1 is a schematic structural diagram of a synthesis gas desorption separation device according to an embodiment of the present utility model.
Reference numerals in the drawings of the specification include: buffer tank 1, composite material conveying pipe 2, condenser 3, conveying pipe 4, distributing pipe 5, recovering pipe 6, buffer pipe 7, return pipe 8, pressure sensor 9, pressure regulating valve 10, liquid level sensor 11, liquid level regulating valve 12, conveying pump 13, purge pipe 14, control valve 15, first baffle 16, second baffle 17.
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, one embodiment of the present utility model provides a synthesis gas desorption separation apparatus, which includes: a buffer tank 1, a synthetic material conveying pipe 2 and a condenser 3;
The lower end of the buffer tank 1 is connected with one end of a conveying pipe 4, and the other end of the conveying pipe 4 is connected with a rectifying tower;
The synthetic material conveying pipe 2 penetrates through the top wall of the buffer tank 1 and is connected with the distribution pipe 5, the distribution pipe 5 is arranged above the liquid level of the buffer tank 1, and a plurality of through holes are uniformly distributed on the pipe wall of the distribution pipe 5;
The condenser 3 comprises a first space and a second space which are isolated from each other, the first space is used for supplying refrigerant to flow, the upper end of the second space is respectively connected with one end of the recovery pipe 6 and one end of the buffer pipe 7, the other end of the buffer pipe 7 is connected with the upper end of the buffer tank 1, the lower end of the second space is connected with one end of the return pipe 8, and the other end of the return pipe 8 penetrates through the top wall of the buffer tank 1 and extends below the liquid level of the buffer tank 1.
The working process of the synthesis gas desorption and separation device is as follows:
The cold hydrogenation synthetic material is conveyed to the buffer tank 1 through the synthetic material conveying pipe 2, sprayed out to the gas-phase space of the buffer tank 1 in a mist form through a plurality of through holes of the distribution pipe 5, so that the synthetic material liquid drops are dispersed, the desorption of hydrogen in the synthetic material is facilitated, gas-phase fluid in the buffer tank 1 is conveyed to the second space of the condenser 3 through the buffer pipe 7, chlorosilane in the gas-phase fluid is condensed under the action of a refrigerant, and returned to the buffer tank 1 through the return pipe 8, and the gas-liquid separation of hydrogen and chlorosilane in the synthetic material is realized.
Moreover, because the other end of the return pipe 8 extends below the liquid level of the buffer tank 1, the gas-phase fluid in the buffer tank 1 is prevented from entering the return pipe 8, so that the buffer tank 1, the buffer pipe 7, the condenser 3 and the return pipe 8 form a chlorosilane condensation recovery passage, the separation efficiency of hydrogen and chlorosilane is improved, and the desorption and recovery efficiency of hydrogen is improved.
Specifically, the refrigerant is circulating water, 7 ℃ water and flowing air, and the chlorosilane in the gas-phase fluid entering the condenser 3 is condensed.
Specifically, the device is used for desorbing the hydrogen dissolved in the synthetic material in the production process of the cold hydrogenation working section, and the hydrogen returns to the cold hydrogenation working section for recycling through the recovery pipe 6, so that the production cost is reduced.
Specifically, after desorbing hydrogen, the cold hydrogenation synthesis material is beneficial to rectification separation in a later section, ensures the stability of the technical parameters of the rectifying tower and the operation of the rectifying tower, and improves the purity of the rectifying separation chlorosilane.
Specifically, above the liquid level in the buffer tank 1, the synthetic material fluid is atomized and sprayed out through a plurality of through holes of the distribution pipe 5, which is beneficial to desorption of hydrogen.
Specifically, the pressure of the cold hydrogenation synthesis pipeline is 2.5MPa, the temperature is about 60 ℃, the pressure of the buffer tank 1 is set to be 0.20-0.30MPa, and the hydrogen dissolved in the chlorosilane is greatly desorbed due to the sudden pressure reduction in the buffer tank 1.
Specifically, the condenser 3 is located above the buffer tank 1.
In the specific embodiment, as shown in fig. 1, the distribution pipe 5 is in a ring shape, and the distribution pipe 5 is horizontally disposed in the buffer tank 1.
In this embodiment, specifically, the distribution pipe 5 is annular and horizontally arranged, and on this basis, as long as the liquid level in the buffer tank 1 is controlled to be below the distribution pipe 5, a plurality of through holes on the distribution pipe 5 are not submerged; the distribution pipe 5 is annular, so that the pipe wall of the distribution pipe 5 can be distributed with through holes as many as possible, the atomization degree of the synthetic material fluid is ensured, and the desorption of hydrogen is promoted.
In a specific embodiment, as shown in fig. 1, the condenser 3 is a horizontal tube heat exchanger, the first space is a tube side of the tube heat exchanger, and the second space is a shell side of the tube heat exchanger.
In this embodiment, specifically, the stroke length of the shell side is longer than that of the tube side, the gas phase fluid to be condensed passes through the shell side of the horizontal tube heat exchanger, the residence time is longer, and the condensation time of chlorosilane in the gas phase fluid is longer, so that the gas-liquid separation efficiency of hydrogen and chlorosilane is improved, and the desorption efficiency of hydrogen is improved.
Specifically, a plurality of first baffle plates 16 and a plurality of second baffle plates 17 are arranged in the shell side of the horizontal tube heat exchanger, the first baffle plates 16 and the second baffle plates 17 are arranged in a staggered mode, wherein the upper ends of the first baffle plates 16 are attached to the top wall of the shell side of the horizontal tube heat exchanger, the lower ends of the second baffle plates 17 are attached to the bottom wall of the shell side of the horizontal tube heat exchanger, and through holes are formed in the edges of the lower ends of the second baffle plates 17. In the running process of the device, gas-phase fluid flows in a folded shape in the shell side of the horizontal type tubular heat exchanger, and condensed chlorosilane is settled at the bottom of the shell side and concentrated to the return pipe 8 through the through hole, so that the gas-phase fluid returns to the buffer tank 1.
In particular, an air cooler may be used for the condenser 3.
As shown in fig. 1, in the specific embodiment, the system further includes a pressure sensor 9 and a pressure regulating valve 10, the pressure sensor 9 is installed at the upper end of the buffer tank 1, the pressure regulating valve 10 is installed at the recovery pipe 6, and the pressure sensor 9 and the pressure regulating valve 10 are integrated in a DCS control system.
In this embodiment, specifically, when the pressure sensor 9 detects that the air pressure in the buffer tank 1 is high, the DCS controller sends an instruction to the pressure regulating valve 10 to increase the opening of the pressure regulating valve 10, so that the pressure in the second space of the condenser 3 and the buffer tank 1 is synchronously reduced to a set range, which is beneficial to condensing and recovering chlorosilane entrained in hydrogen.
As shown in fig. 1, in the specific embodiment, the device further comprises a liquid level sensor 11 and a liquid level regulating valve 12, wherein the liquid level sensor 11 is installed in the buffer tank 1, the liquid level regulating valve 12 is installed in the conveying pipe 4, and the liquid level sensor 11 and the liquid level regulating valve 12 are integrated in a DCS control system.
In this embodiment, specifically, the liquid level sensor 11 adopts the radar level gauge, sets up in the top of buffer tank 1, and when liquid level sensor 11 monitored that the liquid level of buffer tank 1 is higher, the DCS controller sent the instruction to liquid level control valve 12, makes the aperture grow of liquid level control valve 12 to make the material in the buffer tank 1 discharge soon through conveying pipeline 4, make the liquid level of buffer tank 1 drop to the settlement scope, guarantee that the liquid level is stable in the position below distribution pipe 5.
Specifically, the buffer tank further comprises a conveying pump 13, an inlet of the conveying pump 13 is connected to the lower end of the buffer tank 1, and an outlet of the conveying pump 13 is connected to the conveying pipe 4 and is used for providing power for discharging materials in the buffer tank 1.
As shown in fig. 1, in the specific embodiment, the buffer tank 1 further includes a purge pipe 14, and the purge pipe 14 is connected to an upper end of the buffer tank 1.
In this embodiment, specifically, before the device is put into use or when maintenance is required, nitrogen is introduced into the buffer tank 1 through the purge pipe 14, so that the buffer tank 1 is replaced conveniently, and safety is ensured.
In the specific embodiment, as shown in fig. 1, a control valve 15 is further included, and the control valve 15 is mounted to the purge pipe 14.
In the present embodiment, specifically, the control valve 15 is a remote control valve 15, and when the surge tank 1 leaks, the control valve 15 is remotely opened and replaced with nitrogen gas.
In the specific embodiment, as shown in fig. 1, the buffer tank 1 adopts a spherical kettle.
In this embodiment, the spherical kettle has better pressure bearing, so that the pressure resistance of the buffer tank 1 is better, and the leakage probability of the buffer tank 1 is reduced.
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 (8)
1. A synthesis gas stripping and separation device, comprising:
The lower end of the buffer tank is connected with one end of a conveying pipe, and the other end of the conveying pipe is connected with the rectifying tower;
The synthetic material conveying pipe penetrates through the top wall of the buffer tank and is connected with the distribution pipe, the distribution pipe is arranged above the liquid level of the buffer tank, and a plurality of through holes are uniformly distributed in the pipe wall of the distribution pipe;
the condenser, the condenser includes first space and the second space of mutual isolation, first space is used for supplying the refrigerant to flow, the upper end in second space is connected in the one end of recovery tube and buffer tube's one end respectively, the other end in buffer tube the upper end of buffer tank, the lower extreme in second space is connected in the one end of back flow, the other end of back flow runs through the roof of buffer tank, and extends to under the liquid level of buffer tank.
2. The synthesis gas stripping and separating device as claimed in claim 1, wherein,
The distribution pipe is annular, and the distribution pipe is horizontally arranged in the buffer tank.
3. The synthesis gas stripping and separating device as claimed in claim 1, wherein,
The condenser is a horizontal type tube nest heat exchanger, the first space is the tube side of the tube nest heat exchanger, and the second space is the shell side of the tube nest heat exchanger.
4. The synthesis gas stripping and separating device as claimed in claim 1, wherein,
The system also comprises a pressure sensor and a pressure regulating valve, wherein the pressure sensor is arranged at the upper end of the buffer tank, the pressure regulating valve is arranged in the recovery pipe, and the pressure sensor and the pressure regulating valve are integrated in the DCS control system.
5. The synthesis gas stripping and separating device as claimed in claim 1, wherein,
Still include level sensor and liquid level control valve, level sensor install in the buffer tank, liquid level control valve install in the conveying pipeline, level sensor with the liquid level control valve is integrated in the DCS control system.
6. A synthesis gas stripping and separating device as claimed in any of claims 1 to 5, characterized in that,
The buffer tank further comprises a purging pipe, and the purging pipe is connected to the upper end of the buffer tank.
7. The synthesis gas stripping and separating device as claimed in claim 6, characterized in that,
The device also comprises a control valve, wherein the control valve is arranged on the purging pipe.
8. A synthesis gas stripping and separating device as claimed in any of claims 1 to 5, characterized in that,
The buffer tank adopts a spherical kettle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323089720.3U CN221191574U (en) | 2023-11-16 | 2023-11-16 | Synthetic material gas desorption separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323089720.3U CN221191574U (en) | 2023-11-16 | 2023-11-16 | Synthetic material gas desorption separator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221191574U true CN221191574U (en) | 2024-06-21 |
Family
ID=91517636
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202323089720.3U Active CN221191574U (en) | 2023-11-16 | 2023-11-16 | Synthetic material gas desorption separator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN221191574U (en) |
-
2023
- 2023-11-16 CN CN202323089720.3U patent/CN221191574U/en active Active
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