CN220405211U - Adsorption tower heat recycling device - Google Patents
Adsorption tower heat recycling device Download PDFInfo
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- CN220405211U CN220405211U CN202322023191.0U CN202322023191U CN220405211U CN 220405211 U CN220405211 U CN 220405211U CN 202322023191 U CN202322023191 U CN 202322023191U CN 220405211 U CN220405211 U CN 220405211U
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- adsorption tower
- hydrogen
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- adsorption
- pipe
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 89
- 238000004064 recycling Methods 0.000 title abstract description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 59
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 58
- 239000001257 hydrogen Substances 0.000 claims abstract description 58
- 238000007664 blowing Methods 0.000 claims abstract description 19
- 238000007599 discharging Methods 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000000498 cooling water Substances 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 abstract description 16
- 230000008929 regeneration Effects 0.000 abstract description 13
- 238000011069 regeneration method Methods 0.000 abstract description 13
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 229910021420 polycrystalline silicon Inorganic materials 0.000 abstract description 5
- 229920005591 polysilicon Polymers 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 23
- 238000001816 cooling Methods 0.000 description 10
- 239000003463 adsorbent Substances 0.000 description 7
- 239000012535 impurity Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 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 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 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
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000005049 silicon tetrachloride 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
Abstract
The utility model discloses an adsorption tower heat recycling device, relates to the technical field of polysilicon production, and mainly aims to improve the comprehensive heat utilization efficiency in the regeneration process of a hydrogen adsorption tower. The main technical scheme of the utility model is as follows: the embodiment of the utility model provides an adsorption tower heat recycling device, which comprises: the shaft sides of the adsorption towers A, B, C are respectively provided with heat exchange coils; one end of the hydrogen main pipe is respectively connected with the upper end of the adsorption tower A, B, C; one end of the hydrogen back-blowing pipe is respectively connected with the upper end of the adsorption tower A, B, C; one end of the back-blowing discharging pipe is respectively connected with the lower end of the adsorption tower A, B, C; the heat exchanger comprises a first space and a second space which are isolated from each other, the other end of the hydrogen main pipe is connected to an inlet of the first space, the other end of the hydrogen back-blowing pipe is connected to an outlet of the first space, the other end of the back-blowing discharging pipe is connected to an inlet of the second space, and an outlet of the second space is connected to subsequent heat exchange equipment.
Description
Technical Field
The utility model relates to the technical field of polysilicon production, in particular to an adsorption tower heat recycling device.
Background
The polysilicon production adopts an improved Siemens method, and a tail gas recovery workshop mostly adopts a dry recovery process. The tail gas sent by a reduction workshop is mainly treated, the tail gas contains mixed high-temperature gas of trichlorosilane, dichlorosilane, silicon tetrachloride, hydrogen and hydrogen chloride, after the tail gas is subjected to deep cooling, the separated hydrogen enters an absorption tower through a compression system, the hydrogen is leached and purified, impurities such as HCL and the like contained in the hydrogen are absorbed, and the hydrogen is led to the absorption tower for further impurity removal, so that a qualified reduction hydrogen raw material is provided.
In the existing process flow, in a pressure swing adsorption system, 3 adsorption towers are a set of towers (A, B, C), and adsorbents in the towers are adsorbed for a long time to reach a saturated state in the operation process, so that the states of the three towers in the operation process are that the low-temperature adsorption temperature A is generally about 7 ℃, the heating regeneration temperature of the tower B is controlled to be about 180 ℃, the cooling standby of the tower C is generally about 7 ℃, the adsorption, the regeneration and the cooling standby of the three towers A, B, C are alternately carried out, and the regenerated and reversely blown hydrogen (145 ℃) is discharged from the bottom of the adsorption tower and then directly sent to a subsequent heat exchange device to be sent to the next process through circulating water cooling, and the heat exchange load of the subsequent heat exchange device is large.
Disclosure of Invention
In view of this, the embodiment of the utility model provides a heat recycling device for an adsorption tower, which mainly aims to improve the comprehensive heat utilization efficiency in the regeneration process of a hydrogen adsorption tower and reduce the heat load of subsequent heat exchange equipment.
In order to achieve the above purpose, the present utility model mainly provides the following technical solutions:
the embodiment of the utility model provides an adsorption tower heat recycling device, which comprises: the device comprises a hydrogen main pipe, a hydrogen back-blowing pipe, a back-blowing discharging pipe, a heat exchanger, an adsorption tower A, an adsorption tower B and an adsorption tower C which are arranged in parallel;
the shaft sides of the adsorption towers A, B, C are respectively provided with heat exchange coils;
one end of the hydrogen main pipe is respectively connected with the upper end of the adsorption tower A, B, C;
one end of the hydrogen back-blowing pipe is respectively connected with the upper end of the adsorption tower A, B, C;
one end of the back-blowing discharging pipe is respectively connected with the lower end of the adsorption tower A, B, C;
the heat exchanger comprises a first space and a second space which are isolated from each other, the other end of the hydrogen main pipe is connected with an inlet of the first space, the other end of the hydrogen blowback pipe is connected with an outlet of the first space, the other end of the blowback discharging pipe is connected with an inlet of the second space, and an outlet of the second space is connected with subsequent heat exchange equipment.
The aim and the technical problems of the utility model can be further realized by adopting the following technical measures.
Optionally, the adsorption towers A, B, C are respectively provided with heat exchange coils, and the heat exchange coils are respectively connected with a cooling water mechanism and a hot water mechanism.
Optionally, a hydrogen feeding pipe is further included, and the hydrogen feeding pipes are respectively connected to the lower ends of the adsorption towers A, B, C.
Optionally, the cooling water mechanism is a 7 ℃ cooling water mechanism, and the hot water mechanism is a 180 ℃ hot water mechanism.
By means of the technical scheme, the utility model has at least the following advantages:
assuming that at a certain moment of operation of the pressure swing adsorption system, the adsorption tower A performs low-temperature adsorption, the adsorption tower B performs heating regeneration, the adsorption tower C performs cooling for standby, pure hydrogen generated by the adsorption tower A enters a hydrogen main pipe, part of pure hydrogen in the hydrogen main pipe enters a first space of a heat exchanger, then enters the adsorption tower B through a hydrogen blowback pipe, and after heat in the adsorption tower B is absorbed by the blowback hydrogen, regenerated gas is formed and reaches a second space of the heat exchanger through a blowback discharge pipe.
In the heat exchanger, the heat of the regenerated gas in the second space is transferred to the back-blowing hydrogen in the first space, so that the back-blowing hydrogen is preheated, then the adsorbent in the adsorption tower B is back-blown, and the temperature is raised again, because the hydrogen is preheated, the temperature in the adsorption tower B can be raised to the regeneration requirement temperature more quickly, and the adsorbent can be regenerated more thoroughly in the same time.
Meanwhile, the temperature of the regenerated gas after heat exchange is reduced, and then the regenerated gas enters the subsequent heat exchange equipment, so that the temperature difference between the regenerated gas and the refrigerant is reduced in the subsequent heat exchange equipment, the cooling load of the subsequent heat exchange equipment on the regenerated gas is reduced, the subsequent heat exchange equipment is protected, and the cooling capacity is saved.
The method mainly aims at heat recovery, energy conservation and consumption reduction of the polycrystalline silicon tail gas recovery adsorption system, and the temperature of the regeneration adsorption tower is improved by fully utilizing heat through research and development of a new process, so that the consumption of steam is reduced, the consumption of cold energy (the cold energy mainly comes from a screw machine of a refrigeration system) is also reduced, and the production cost is reduced.
Drawings
Fig. 1 is a schematic structural diagram of an adsorption tower heat recycling device according to an embodiment of the present utility model.
Reference numerals in the drawings of the specification include: the device comprises an adsorption tower A1, an adsorption tower B2, an adsorption tower C3, a hydrogen main pipe 4, a hydrogen blowback pipe 5, a blowback discharge pipe 6, a heat exchanger 7, a subsequent heat exchange device 8, a heat exchange coil 9 and a hydrogen feed pipe 10.
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 an adsorption tower heat recycling apparatus, which includes: the device comprises a hydrogen main pipe 4, a hydrogen back-blowing pipe 5, a back-blowing discharge pipe 6, a heat exchanger 7, an adsorption tower A1, an adsorption tower B2 and an adsorption tower C3 which are arranged in parallel;
the shaft sides of the adsorption towers A1, B2 and C3 are respectively provided with a heat exchange coil 9;
one end of the hydrogen main pipe 4 is respectively connected with the upper ends of the adsorption towers A1, B2 and C3;
one end of the hydrogen back-blowing pipe 5 is respectively connected with the upper ends of the adsorption towers A1, B2 and C3;
one end of the blowback discharge pipe 6 is respectively connected with the lower ends of the adsorption towers A1, B2 and C3;
the heat exchanger 7 comprises a first space and a second space which are isolated from each other, the other end of the hydrogen main pipe 4 is connected to an inlet of the first space, the other end of the hydrogen blowback pipe 5 is connected to an outlet of the first space, the other end of the blowback discharge pipe 6 is connected to an inlet of the second space, and an outlet of the second space is connected to a subsequent heat exchange device 8.
The working process of the adsorption tower heat recycling device is as follows:
assuming that at a certain moment of operation of the pressure swing adsorption system, the adsorption tower A1 is subjected to low-temperature adsorption, the adsorption tower B2 is heated and regenerated, the adsorption tower C3 is cooled for standby, pure hydrogen generated by the adsorption tower A1 enters the hydrogen main pipe 4, part of the pure hydrogen in the hydrogen main pipe 4 enters the first space of the heat exchanger 7, then enters the adsorption tower B2 through the hydrogen blowback pipe 5, and after heat in the adsorption tower B2 is absorbed by the blowback hydrogen, regenerated gas is formed and reaches the second space of the heat exchanger 7 through the blowback discharge pipe 6.
In the heat exchanger 7, the heat of the regeneration gas in the second space is transferred to the blowback hydrogen in the first space, so that the blowback hydrogen is preheated, then the adsorbent in the adsorption tower B2 is blowback, and the temperature is raised again, because the hydrogen is preheated, the temperature can be raised to the regeneration required temperature more quickly in the adsorption tower B2, and the adsorbent can be regenerated more thoroughly in the same time.
Meanwhile, the temperature of the regenerated gas after heat exchange is reduced, and then the regenerated gas enters the subsequent heat exchange equipment 8, so that the temperature difference between the regenerated gas and the refrigerant in the subsequent heat exchange equipment 8 is reduced, the cooling load of the subsequent heat exchange equipment 8 on the regenerated gas is reduced, the subsequent heat exchange equipment 8 is protected, and the cold is saved.
In the technical scheme of the utility model, the method mainly aims at heat recovery, energy conservation and consumption reduction of the polysilicon tail gas recovery adsorption system, and the heat is fully utilized to improve the temperature of the regeneration adsorption tower by developing a new process, so that the consumption of steam is reduced, the consumption of cold energy (the cold energy mainly comes from a screw machine of a refrigeration system) is also reduced, and the production cost is reduced.
Specifically, the heat exchanger 7 and the subsequent heat exchange equipment 8 are all tube-in-tube heat exchangers, the other end of the hydrogen main tube 4 and the other end of the hydrogen back-blowing tube 5 are respectively connected to the tube side of the heat exchanger 7, and the other end of the back-blowing discharging tube 6 is connected to the shell side of the heat exchanger 7.
In a specific embodiment, the adsorption towers A1, B2 and C3 are respectively provided with a heat exchange coil 9, and the heat exchange coils 9 are respectively connected with a cooling water mechanism and a hot water mechanism.
In the present embodiment, specifically, when one of the adsorption towers A1, B2, and C3 adsorbs or is used for cooling, the cooling water mechanism works to circularly supply the cold coal to the heat exchange coil 9; when one of the adsorption towers A1, B2 and C3 is in a regeneration state, the hot water mechanism works to circularly supply the heat medium to the heat exchange coil 9, so that the temperature of the adsorbent is increased.
In the specific embodiment, the device further comprises a hydrogen feeding pipe 10, and the hydrogen feeding pipe 10 is connected to the lower ends of the adsorption towers A1, B2 and C3 respectively.
In this embodiment, specifically, in the previous step, the purified hydrogen gas still contains a trace amount of impurities, and the hydrogen gas containing a trace amount of impurities enters one of the adsorption towers A1, B2 and C3 through the hydrogen feed pipe 10 to perform an adsorption process, thereby removing impurities and generating pure hydrogen.
In a specific embodiment, the cooling water mechanism is a 7 ℃ cooling water mechanism, and the hot water mechanism is a 180 ℃ hot water mechanism.
In the embodiment, in the regeneration process of the adsorption tower, a hot water mechanism at 180 ℃ is operated to heat the adsorbent in the adsorption tower, the regenerated gas discharged from the adsorption tower can be heated to 145 ℃, in the heat exchanger 7, the regenerated gas at 145 ℃ can pull the temperature of the reversely blown gas to 100 ℃, the heat load in the regeneration process of the adsorption tower is reduced, the temperature of the regenerated gas after heat exchange can be reduced to 40 ℃, and the cold energy of the subsequent heat exchange equipment 8 is saved;
specifically, in the process of cooling the adsorption tower for standby, a cooling water mechanism at 7 ℃ operates to reduce the temperature of the adsorption tower.
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 (4)
1. The utility model provides an adsorption tower heat recovery utilizes device which characterized in that includes:
the adsorption tower A, the adsorption tower B and the adsorption tower C are arranged in parallel, and heat exchange coils are respectively arranged on the shaft sides of the adsorption towers A, B, C;
one end of the hydrogen main pipe is respectively connected with the upper end of the adsorption tower A, B, C;
one end of the hydrogen back-blowing pipe is respectively connected with the upper end of the adsorption tower A, B, C;
one end of the back-blowing discharging pipe is respectively connected with the lower end of the adsorption tower A, B, C;
the heat exchanger comprises a first space and a second space which are isolated from each other, the other end of the hydrogen main pipe is connected with an inlet of the first space, the other end of the hydrogen back-blowing pipe is connected with an outlet of the first space, the other end of the back-blowing discharging pipe is connected with an inlet of the second space, and an outlet of the second space is connected with subsequent heat exchange equipment.
2. The heat recovery and utilization device of an adsorption tower according to claim 1, wherein,
the adsorption towers A, B, C are respectively provided with heat exchange coils, and the heat exchange coils are respectively connected with a cooling water mechanism and a hot water mechanism.
3. The heat recovery and utilization device of an adsorption tower according to claim 1, wherein,
the hydrogen gas inlet pipe is respectively connected to the lower ends of the adsorption towers A, B, C.
4. The heat recovery and utilization device of an adsorption tower according to claim 2, wherein,
the cooling water mechanism is a 7 ℃ cooling water mechanism, and the hot water mechanism is a 180 ℃ hot water mechanism.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322023191.0U CN220405211U (en) | 2023-07-31 | 2023-07-31 | Adsorption tower heat recycling device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322023191.0U CN220405211U (en) | 2023-07-31 | 2023-07-31 | Adsorption tower heat recycling device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220405211U true CN220405211U (en) | 2024-01-30 |
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ID=89657370
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322023191.0U Active CN220405211U (en) | 2023-07-31 | 2023-07-31 | Adsorption tower heat recycling device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220405211U (en) |
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2023
- 2023-07-31 CN CN202322023191.0U patent/CN220405211U/en active Active
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