CN218221688U - Heat exchange and separation integrated equipment - Google Patents
Heat exchange and separation integrated equipment Download PDFInfo
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- CN218221688U CN218221688U CN202222072108.4U CN202222072108U CN218221688U CN 218221688 U CN218221688 U CN 218221688U CN 202222072108 U CN202222072108 U CN 202222072108U CN 218221688 U CN218221688 U CN 218221688U
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- separation
- heat exchange
- downcomer
- module
- separation module
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- 238000000926 separation method Methods 0.000 title claims abstract description 122
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 238000004581 coalescence Methods 0.000 claims description 16
- 238000007789 sealing Methods 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 5
- 230000000712 assembly Effects 0.000 claims description 4
- 238000000429 assembly Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 53
- 239000007787 solid Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 10
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 8
- 239000012495 reaction gas Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 6
- 229910000831 Steel Inorganic materials 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- 239000010959 steel Substances 0.000 description 5
- 239000000295 fuel oil Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 230000010354 integration Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000006196 drop Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A heat exchange and separation integrated device is an integrated structure formed by connecting an upper heat exchange module and a lower separation module in a through manner; the separation module consists of a downcomer and a separation internal part; the upper end of the downcomer is communicated with a medium outlet at the hot side of the heat exchange module through a separation module inlet cylinder, and the upper end of the separation module cylinder is hermetically connected with the outer wall of the separation module inlet cylinder; the lower end of the downcomer is provided with a gas diffuser, a separation component supporting frame is sleeved on the downcomer above the gas diffuser in a clearance mode, a separation internal part is installed in the separation component supporting frame, a bottom frame of the separation component supporting frame is provided with a through hole, the through hole is communicated with the downcomer, and the other end of the downcomer extends to a position below the lowest liquid level of the lower end of the separation module barrel. The utility model discloses reduce gas temperature, improved gaseous quality, played effectual protection to low reaches treatment facility.
Description
Technical Field
The utility model relates to a heat transfer separation technical field especially relates to a heat transfer separation integration equipment that uses in the normal butane oxidation legal system maleic anhydride technology of chemical industry.
Background
The heat exchange separation is an important component of the technology for preparing maleic anhydride by using the n-butane oxidation method, the low-temperature and pure reaction gas is obtained, one of the important processes for preparing the maleic anhydride by using the n-butane oxidation method, the heat exchange separator is key equipment of the technology, and the performance of the heat exchange separator directly influences the safe and stable operation of a maleic anhydride production system.
The heat exchange separation device has the main functions in the maleic anhydride production system as follows: reducing the temperature of the reaction gas, and separating liquid and solid catalyst particles in the reaction gas. The basic process flow is as follows: the high-temperature reaction gas enters a heat exchange module to exchange heat with a refrigerant; the cooled high-temperature reaction gas enters a separation module to complete gas-liquid-solid separation. The heat exchange separation device commonly used in the industry consists of a heat exchange module and a separation module. Wherein, the heat exchange module structure adopts a shell-and-tube heat exchanger; the main separation elements of the separation module are a cyclonic separation element and a liquid coalescing element.
A common cyclone separation element, such as Chinese patent 202110522996.2, discloses a high-efficiency heat exchange separator, which uses a cyclone tube to separate liquid and solid particles in gas, reduces the gas temperature, improves the gas dryness and effectively protects subsequent treatment equipment. But the device only has one-time separation, the separation efficiency is low, the pressure drop of the device is large, and the energy consumption is high.
Common liquid coalescence elements, such as pall rings, have the problems of easy blockage of separators, downstream solvent pollution and the like, so that equipment is frequently switched, the labor intensity is high, unsafe factors are increased, and production waste is increased. The heat exchange separation device has the advantages of large floor area, single separation method and low separation efficiency. To achieve higher separation efficiency, higher energy consumption is generally required.
Chinese patent 201821864709.6 discloses a separator internal part of a circulating heat exchange separator, which utilizes the principle of cyclone separation to separate heavy oil and catalyst particles carried by gas, and utilizes a coalescence plate to coalesce and separate gas containing liquid, thereby ensuring the safe and stable operation of the separation functional section of the circulating heat exchange separator. Although the device combines two methods of cyclone separation and coalescence separation, the device structure is not reasonable, the performance of the cyclone separation element can not be fully exerted, and the energy consumption is still high.
In addition, the method for preparing maleic anhydride by the n-butane oxidation method has the disadvantages of complex reaction gas components, high corrosivity, easy adhesion and coke formation, and serious influence on the operation cycle and the service life of the heat exchange separation device.
SUMMERY OF THE UTILITY MODEL
The utility model provides a heat transfer separation integration equipment to solve area that traditional gas-liquid heat transfer separation process units exists big, the inefficiency, easily block up, life weak point and maintain technical problem such as complicacy.
The utility model discloses the technical scheme who adopts does:
a heat exchange and separation integrated device is an integrated structure formed by connecting an upper heat exchange module and a lower separation module in a through manner; the separation module consists of a downcomer and a separation internal part in a separation module cylinder body; the upper end of the downcomer is communicated with a medium outlet at the hot side of the heat exchange module through a separation module inlet cylinder, and the upper end of the separation module cylinder is hermetically connected with the outer wall of the separation module inlet cylinder; the lower end of the downcomer is provided with a gas diffuser, a separation component support frame is sleeved on the downcomer in a clearance mode above the gas diffuser, a separation internal part is installed in the separation component support frame, the upper end of the separation component support frame is sealed by a support frame top sealing plate, the space between the outer edge of a bottom frame of the lower end and the inner wall of a separation module barrel body is sealed by a support frame lower portion annular sealing partition plate, a through hole is formed in the bottom frame of the separation component support frame and is in through connection with the downcomer, and the other end of the downcomer extends to a position below the lowest liquid level of the lower end of the separation module barrel body.
The lower end of the downcomer is in cross-symmetric radial connection with a gas diffuser.
The gas diffuser is integrally installed downwards obliquely from the center to the outside, and the downward oblique angle is 10-15 degrees.
And a gas vortex breaker is arranged at a gas outlet of the separation module at the upper part of the separation module cylinder.
The separation internals are coalescence corrugated plates which are annular coalescence plates with radial channels, and the fluid channels narrow in and wide out in the direction from the inlet to the outlet of the radial channels.
At least one group of spraying assemblies is arranged in a channel from a hot-side medium outlet of the heat exchange module to the front of the coalescent corrugated plate.
The utility model has the advantages that: the temperature of the gas is reduced, the gas dryness is improved, and the downstream treatment equipment is effectively protected. And the device has simple and compact structure, large treatment capacity, small occupied area, convenient operation and reliable performance, and the continuous service time of a single device is more than 12 months. The heat exchange and separation efficiency is high, the removal rate of solid dust in the reaction gas at the outlet of the separator is 99.999 percent, the tar content is less than 0.1PPm, and the removal rate of liquid drops with the particle size larger than 5 mu m is more than 99.5 percent. The utility model is particularly suitable for the gas-liquid treatment process of preparing maleic anhydride and the like by the n-butane oxidation method in the chemical field.
Drawings
FIG. 1 is a schematic view of the present invention;
fig. 2 is a top view of the separation module of the present invention;
FIG. 3 is a schematic view of the separation module support frame of the present invention;
fig. 4 is a schematic view of the arrangement of the coalesced corrugated plate of the present invention;
FIG. 5 is a schematic view of a gas diffuser according to the present invention;
numbering in the figures: 1-skirt 2-separation module, 3-heat exchange module, 4-heat exchange module cylinder, 5-hot side medium inlet, 6-hot side medium outlet, 7-separation module gas outlet, 8-separator drain outlet, 9-spray outlet, 10-cold side medium outlet, 11-cold side medium inlet, 12-spray assembly, 13-coalescence corrugated plate, 14-gas diffuser, 15-downcomer, 16-liquid eddy device, 17-1,17-2-first and second equipment connecting flange 18-downcomer, 19-gas eddy device, 20-manhole, 21-separation assembly supporting frame, 22-supporting frame top sealing plate, 23-separation module cylinder, 24-separation module inlet cylinder wall, 25-supporting frame lower part annular sealing partition plate.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings.
Referring to fig. 1, the heat exchange and separation integrated equipment is an integrated structure formed by connecting an upper heat exchange module 3 and a lower separation module 2 in a penetrating manner and is supported by a skirt 1; the heat exchange module 3 comprises but is not limited to a shell-and-tube heat exchanger, the upper end of the heat exchange module 3 is connected with the heat exchange module cylinder 4 through a first equipment flange 17-1, and the top of the heat exchange module cylinder 4 is provided with a hot-side medium inlet 5; the lower end of the heat exchange module 3 is communicated with the separation module inlet cylinder 24 through a second equipment flange 17-2; a cold side medium inlet 11 is arranged at the lower part of the heat exchange module 3, and a cold side medium outlet 10 is arranged at the upper part of the heat exchange module 3; the separation module 2 consists of a downcomer 18 and a separation internal part in a separation module cylinder body; the upper end of the downcomer 18 is communicated with the hot-side medium outlet 6 of the heat exchange module 3 through a separation module inlet cylinder 24, and the upper end of the separation module cylinder is hermetically connected with the outer wall of the separation module inlet cylinder 24; the lower end of the downcomer 18 is provided with a gas diffuser 14, a separation component support frame 21 is sleeved on the downcomer 18 above the gas diffuser 14 in a clearance mode, a separation internal part is installed in the separation component support frame 21, the upper end of the separation component support frame 21 is sealed by a support frame top sealing plate 22, the outer edge of a bottom frame at the lower end and the inner wall of a separation module cylinder body are sealed by a support frame lower annular sealing partition plate 25, a through hole is formed in the bottom frame of the separation component support frame 21 and is in through connection with the downcomer 15, and the other end of the downcomer 15 extends to be below the lowest liquid level of the lower end of the separation module cylinder body. The bottom of the cylinder body of the separation module is provided with a sewage outlet 8, and the bottom of the side of the cylinder body is provided with a manhole 20.
The size of each element is determined according to the upstream heat exchange gas treatment capacity and characteristics.
The lower end of the downcomer 18 is cross-symmetrically radially connected to the gas diffuser 14.
The gas diffuser 14 is integrally installed downwards in an inclined mode from the center to the outside, the inclined angle is 10-15 degrees, and solid particles or liquid with high viscosity can slide downwards to a sewage discharge area.
And a gas vortex breaker 19 is arranged at the gas outlet 7 of the separation module at the upper part of the separation module cylinder body to prevent the gas from deviating and carrying entrainment.
The utility model discloses a gas diffuser 14 as shown in fig. 5, by roof, bottom plate and a plurality of crooked blade component, the blade component divide into two, one is crooked left, one is crooked right. The inlet medium mixed fluid rapidly expands along the distribution direction of the blades, so that the gas rapidly escapes from the liquid, and the inlet device has the advantage of eliminating the impact of high-speed fluid on the wall of the container so as to reduce disturbance. So that the liquid and the solid are settled to the bottom of the equipment, and the gas forms stable laminar flow and enters a coalescence corrugated plate separation component.
At least one group of spraying assemblies 12 are arranged in the passage from the hot side medium outlet 6 of the heat exchange module 3 to the front of the gas diffuser 14. The spray component 12 is composed of an inlet connecting pipe, a circular ring pipe and a nozzle, the circular ring pipe is coaxially arranged inside the descending pipe, the inlet connecting pipe enters the circular ring pipe through the cylinder wall, and the nozzle is positioned at the bottom of the circular ring pipe. The spraying assembly has the functions of: the solubility of liquid and solid such as heavy oil, catalyst and the like in gas is reduced, and the separation of the liquid and the solid from the gas is facilitated; while flushing the separation module inlet cylinder 24 to prevent heavy oil from adhering to the walls. The spray assemblies can be arranged in one group or two groups according to the requirement.
The separation internals are coalescence corrugated plates 13 which mainly function to coalesce and separate liquid and solid. The coalescence corrugated plate 13 is a coalescence plate with a ring shape and radial channels, the fluid channel is narrow in and wide out in the direction from the inlet to the outlet of the radial channels, the center of the radial channels is a gas channel, and gas to be separated is coalesced and separated from inside to outside. The circular separating internal part composed of the coalescence corrugated plates is beneficial to liquid-solid collision coalescence separation at an inlet because the flow channel is narrow and the flow rate of a medium is high; and along with the continuous change of the flowing direction and the flowing section, the liquid and the solid are separated from the airflow because the original moving direction is kept by large inertia, a liquid film is formed on the wall surface of the blade, and the liquid film is settled and separated downwards along the wall surface of the blade under the action of gravity. At the flow channel outlet, the medium flow channel is widened, the flow speed is reduced, the liquid film is favorably coalesced and settled to the bottom of the liquid, and the entrainment of gas mist is prevented.
The downcomer 15 serves to divert liquid separated by the coalesced corrugated sheet 13 below a minimum liquid level. The number and size of downcomers 15 is determined by the upstream heat exchange gas throughput and liquid content.
The annular sealing partition 25 at the lower part of the supporting frame is an annular thin plate and is used for preventing back mixing of gas and liquid before and after separation.
The downcomer 18 is a thin-walled cylindrical structure and is configured to receive the liquid-solid-containing high-temperature gas after the top heat exchange module is cooled.
The separation assembly support frame 21 is a circular frame formed by splicing channel steel or steel plates, and a groove-shaped frame formed by the channel steel or the steel plates is used for placing the corrugated coalescence plates.
The supporting frame top sealing plate 22 is an annular steel plate, the outer edge of the supporting frame top sealing plate is connected with the outer edge of the separating assembly supporting frame, and the edge of the inner cavity is connected with the outer wall of the downcomer; which acts to force the incompletely separated gases through the coalescing plates for separation.
The utility model discloses equipment is the pressure-bearing casing.
The utility model discloses a theory of operation:
referring to fig. 1, after heat exchange is performed on a hot-side medium (high-temperature gas containing liquid and solid) through the heat exchange module 3, the hot-side medium flows into the inlet of the separation module 2 through the hot-side medium outlet, and the whole process is full-countercurrent heat transfer, so that high heat transfer efficiency is ensured. The high temperature gas containing liquid and solid is cleaned and cooled by the spraying component 12, the gas and the liquid and solid are conveyed to a gas diffuser through a downcomer 18, and the feeding fluid is forcibly separated through a plurality of bent blade runners. When gas carries liquid and solid to flow in the blade flow passage, the inertia of spray liquid drops, heavy oil and catalyst particles is larger than that of the gas, the tiny liquid and solid is separated from the gas flow under the action of gravity and centrifugal force and collides with the wall surface of the blade to be trapped, and the tiny liquid and solid is initially separated from the gas under the action of gravity and collision coalescence. The primarily separated gas enters the series of coalesced corrugated plates 13 uniformly through the gap between the downcomer and the separation module support frame 21.
The gas is forced to pass through the narrow gap channels formed by the coalescence corrugated plates 13, which provide the opportunity for the droplets in the gas to collide and coalesce sufficiently frequently and adhere to the plates to coalesce, so that the small droplets in the gas form large droplets, which ultimately form a flow of detergent liquid to the bottom of the separation assembly support frame 21 and then to below the lowest level of the bottom of the cylinder via the downcomer 15; the separated gas flows to the upper part of the separation component supporting frame 21 and then is discharged out of the cylinder of the separation module 2 through the gas vortex breaker 19 and the gas outlet 7 of the separation module, thereby finally achieving the purpose of gas-liquid separation.
The embodiments described above are presented to enable a person of ordinary skill in the art to make and use the invention. It will be readily apparent to those of ordinary skill in the art that various modifications to these embodiments and the generic principles defined herein may be applied to other fields without the use of the inventive faculty. Therefore, the present invention is not limited to the above examples, and is not limited to the technical field of maleic anhydride production. In light of the present disclosure, it is intended that all such modifications and variations be included within the scope of the invention.
Claims (6)
1. The heat exchange and separation integrated equipment is characterized in that the equipment is an integrated structure formed by connecting an upper heat exchange module (3) and a lower separation module (2) in a through manner; the separation module (2) consists of a downcomer (18) and a separation internal part in a separation module cylinder body; the upper end of the downcomer (18) is communicated with a medium outlet (6) at the hot side of the heat exchange module (3) through a separation module inlet cylinder (24), and the upper end of the separation module cylinder is hermetically connected with the outer wall of the separation module inlet cylinder (24); the gas diffuser (14) is installed at the lower end of the downcomer (18), a separation component supporting frame (21) is sleeved on the downcomer (18) above the gas diffuser (14) in a clearance mode, a separation internal part is installed in the separation component supporting frame (21), the upper end of the separation component supporting frame (21) is sealed by a supporting frame top sealing plate (22), the outer edge of the bottom frame of the lower end and the inner wall of the separation module cylinder body are sealed by a supporting frame lower portion annular sealing partition plate (25), a through hole is formed in the bottom frame of the separation component supporting frame (21), the through hole is communicated with the downcomer (15), and the other end of the downcomer (15) extends to be below the lowest liquid level of the lower end of the separation module cylinder body.
2. A heat exchange and separation integrated apparatus according to claim 1, wherein the lower ends of the down comer pipes (18) are cross-symmetrically and radially connected with the gas diffuser (14).
3. The integrated heat exchange and separation apparatus according to claim 2, wherein the gas diffuser (14) is installed in a downward inclination from the center to the outside, and the downward inclination angle is 10-15 °.
4. The heat exchange and separation integrated equipment according to claim 1, wherein a gas vortex breaker (19) is arranged at a separation module gas outlet (7) at the upper part of the separation module cylinder.
5. A heat exchange and separation integrated apparatus according to claim 1, characterized in that the separating internals are corrugated coalescing plates (13), the corrugated coalescing plates (13) are annular sheets of coalescing plates having radial channels, and the channels of the fluid narrow in and wide out in the direction from the inlet to the outlet of the radial channels.
6. A heat exchange and separation integrated device according to any one of claims 1 to 5, characterized in that at least one group of spray assemblies (12) is arranged in the passage from the hot side medium outlet (6) of the heat exchange module (3) to the front of the coalescence corrugated plate (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222072108.4U CN218221688U (en) | 2022-08-08 | 2022-08-08 | Heat exchange and separation integrated equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222072108.4U CN218221688U (en) | 2022-08-08 | 2022-08-08 | Heat exchange and separation integrated equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218221688U true CN218221688U (en) | 2023-01-06 |
Family
ID=84679655
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222072108.4U Active CN218221688U (en) | 2022-08-08 | 2022-08-08 | Heat exchange and separation integrated equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218221688U (en) |
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2022
- 2022-08-08 CN CN202222072108.4U patent/CN218221688U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information |
Inventor after: Wen Xiaolong Inventor after: Zhang Shangwen Inventor after: Feng Sensen Inventor after: He Yiming Inventor after: Zhou Shaobin Inventor after: Xie Tengteng Inventor after: Sun Donglai Inventor after: Li Xuanang Inventor after: Li Jinbo Inventor before: Wen Xiaolong Inventor before: Xie Tengteng Inventor before: Sun Donglai Inventor before: Li Xuanang Inventor before: Li Jinbo Inventor before: Zhang Shangwen Inventor before: Zhang Han Inventor before: Feng Sensen Inventor before: Xu Han Inventor before: He Yiming Inventor before: Yang Shansheng Inventor before: Zhou Shaobin Inventor before: Zhong Xiaoping |
|
| CB03 | Change of inventor or designer information | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231010 Address after: 730070 No.8 Lanke Road, Anning District, Lanzhou City, Gansu Province Patentee after: Lanpec Technologies Ltd. Patentee after: SHANGHAI LANBIN PETROCHEMICAL EQUIPMENT Co.,Ltd. Address before: 730070 No.8 Lanke Road, Anning District, Lanzhou City, Gansu Province Patentee before: Lanpec Technologies Ltd. Patentee before: SHANGHAI LANBIN PETROCHEMICAL EQUIPMENT Co.,Ltd. Patentee before: SHANGHAI HOTO ENGINEERING Inc. |
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| TR01 | Transfer of patent right |