CN215516706U - Evaporative crystallization system - Google Patents
Evaporative crystallization system Download PDFInfo
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- CN215516706U CN215516706U CN202121538825.0U CN202121538825U CN215516706U CN 215516706 U CN215516706 U CN 215516706U CN 202121538825 U CN202121538825 U CN 202121538825U CN 215516706 U CN215516706 U CN 215516706U
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- reflux
- inlet
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 27
- 230000008025 crystallization Effects 0.000 title claims abstract description 19
- 239000012452 mother liquor Substances 0.000 claims abstract description 43
- 239000002562 thickening agent Substances 0.000 claims abstract description 43
- 150000003839 salts Chemical class 0.000 claims abstract description 42
- 238000010992 reflux Methods 0.000 claims abstract description 39
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 34
- 230000001105 regulatory effect Effects 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims 1
- 230000008021 deposition Effects 0.000 abstract description 10
- 239000000463 material Substances 0.000 abstract description 7
- 239000012047 saturated solution Substances 0.000 abstract description 5
- 238000009833 condensation Methods 0.000 abstract 1
- 230000005494 condensation Effects 0.000 abstract 1
- 238000007599 discharging Methods 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 12
- 239000000243 solution Substances 0.000 description 6
- 238000011160 research Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005485 electric heating Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000013078 crystal Substances 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 235000013361 beverage Nutrition 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 235000013365 dairy product Nutrition 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000013535 sea water Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an evaporative crystallization system, which comprises a crystallizer, a thickener, a centrifugal machine, a mother liquor tank, a forced heater, a reflux pump, a raw material inlet and a circulating pump, wherein the crystallizer is provided with a feed inlet, a reflux outlet and a discharge outlet, the raw material inlet is connected with the feed inlet after passing through the reflux pump and the forced heater in sequence, the reflux outlet is connected with the raw material inlet, the discharge outlet is connected with the thickener, the discharge outlet of the thickener is connected with the centrifugal machine, the centrifugal machine is provided with a mother liquor outlet and a salt outlet, the mother liquor outlet is connected with the mother liquor tank, the salt outlet is connected with a recovery tank, the bottom of the mother liquor tank is provided with a liquor outlet, the liquor outlet is connected with the reflux inlet through the circulating pump, the outside of the thickener is provided with a condensation pipe, and the top of the thickener is provided with a rotary rake. The system can increase the salt yield of the material in unit time and reduce the useless power circulation. The salt deposition of the saturated solution on the inner wall of the pipeline can be effectively avoided.
Description
Technical Field
The utility model relates to the technical field of water treatment equipment, in particular to an evaporative crystallization system.
Background
The evaporative crystallization technology is required in the industries of food deep processing, dairy industry, industrial wastewater treatment, beverage and the like. The MVR centrifugal salt discharge system is the most advanced evaporative crystallization technology in the prior art, mainly comprises a crystallizer, a thickener, a centrifuge, a mother liquor tank and a reflux system, and has the function of removing a material mixture reaching the supersaturated concentration from the system in a salt form, and the generated mother liquor is a saturated solution and flows back to the interior of the crystallizer for re-concentration.
In the last 70 th century, with the increasing demand for energy and the rapid rise of energy prices, MVR technology has attracted the attention and research of researchers in various countries and has been successfully applied to the operation of evaporation.
In 1957, german GEA company developed a commercial MVR evaporation system for the problem of high energy consumption in the evaporation separation process. In 1999, the U.S. general electric company began to develop MVR for use in heavy oil recovery wastewater evaporation, and in 2004, the U.S. AGV Technologies, in combination with its own technical advantages, developed a new MVR water treatment system named as a wiped film rotary disk, taking into account other MVR Technologies. The traditional mode of each heat transfer surface of the system is changed, and a rotary disk mode is adopted, so that the heat transfer efficiency is improved, the generation of dirt is reduced, the scale of the system is reduced, and the heat transfer coefficient of the system can reach 25 kW.M-2.DEG-1.
In addition to the above-mentioned major institutions, MVR water treatment technologies have been also applied, researched and popularized by GIG Kapasek of Austria, EVATHERM of Switzerland, MAN Diesel ﹠ Turbo of Germany, and the like. Some countries in the middle east are dedicated to the application research of the MVR technology in the field of seawater desalination. It is clear that the MVR technology has received wide attention from the field of foreign water treatment, and is continuously recognized and applied, especially in the field of seawater desalination. Statistically, MVR technology accounts for about 33% of the share in thermal separation systems worldwide.
The MVR technology is introduced into the Chinese market from North America and Europe from 2007, and is mainly applied to industries such as food deep processing, dairy industry, industrial wastewater treatment and beverage. Meanwhile, the technology is continuously researched by colleges and scientific research institutes in China, and the research on MVR is theoretically and practically conducted by Nanjing aerospace university, Western's transport university, Chinese academy physicochemical technology research institute, Beijing industry university, Beijing aerospace university and the like. Since 2008, with the increasing call for environmental protection and energy conservation, MVR started the rise of the platform, and a large number of reports were applied to commercial practice.
At present, the MVR salt discharge system in the industry mainly comprises the following systems:
(1) and continuously discharging salt, setting the opening degree of a discharge valve of the crystallizer, continuously discharging the feed liquid to the thickener, enabling the thickener to overflow from the top to enter a mother liquid tank, and continuously discharging the salt in the thickener.
(2) And (3) discharging salt discontinuously, opening a discharge valve of the crystallizer discontinuously to discharge the feed liquid to the thickener, closing the discharge valve after the thickener is filled with the feed liquid every time, discharging the salt through standing and cooling measures, and then discharging the salt through the thickener.
(3) The outlet of the mother liquor reflux pump is provided with an internal reflux, the outlet of the pump directly refluxes into the mother liquor tank, and when the liquid level of the mother liquor tank is high, the valve is opened again to reflux into the crystallizer.
The prior art mainly has the following defects:
(1) whether continuous salt discharging or intermittent salt discharging is carried out, the salt deposition problem is easy to occur on the salt discharging pipe wall, the intermittent salt discharging is particularly serious, and if no measures are taken, the problem that the flow of a pipeline is limited or even the material cannot be discharged is easily caused.
(2) Whether the salt is continuously discharged or discontinuously discharged, the inside of the thickener is a mixture of crystallization and material saturated solution, and the amount of the salt discharged by real centrifugation is limited.
The problems to be solved in the prior art are mainly:
1. increase the crystal yield in the thickener and reduce the reflux of the mother liquor.
2. Solves the problem that the salt outlet pipeline and the mother liquid return pipeline are easy to block.
Disclosure of Invention
Aiming at the defects of the prior art, the evaporative crystallization system is developed, and the evaporative crystallization system is high in crystallization efficiency, high in yield and less in pipeline blockage faults.
The technical scheme for solving the technical problem of the utility model is as follows: on one hand, the embodiment of the utility model provides an evaporative crystallization system which comprises a crystallizer, a thickener, a centrifugal machine, a mother liquor tank, a forced heater, a reflux pump, a raw material inlet and a circulating pump, wherein the crystallizer is provided with a feed inlet, a reflux outlet and a discharge port, the raw material inlet is connected with the feed inlet after passing through the reflux pump and the forced heater in sequence, the reflux outlet is connected with the raw material inlet, the discharge port is connected with the thickener, the discharge port of the thickener is connected with the centrifugal machine, the centrifugal machine is provided with a mother liquor outlet and a salt outlet, the mother liquor outlet is connected with the mother liquor tank, the salt outlet is connected with a recovery tank, the bottom of the mother liquor tank is provided with a liquor outlet, the liquor outlet is connected with the reflux inlet through the circulating pump, a condensing pipe is arranged outside the thickener, and a rotary rake is arranged at the top of the thickener.
Preferably, the condenser pipe wraps a shell of the thickener, the condenser pipe is provided with a cold water inlet and a cold water outlet, the cold water inlet is arranged at the lower part, and the cold water outlet is arranged at the upper part.
Preferably, the rotary rake comprises a motor and a rake rod, the motor is mounted at the top of the thickener, the rake rod is connected with an output shaft of the motor, and the rake rod is inserted into the thickener.
Preferably, a regulating valve is further arranged on a pipeline between the liquid outlet and the reflux inlet.
Preferably, the regulating valve is positioned at a reflux inlet.
As optimization, valves are arranged on the front pipeline and the rear pipeline of the regulating valve. The regulating valve can be protected.
As optimization, both ends of the regulating valve are also provided with standby pipelines, and valves are arranged on the standby pipelines. A condensing pipe is arranged on the upper surface of the shell,
preferably, the mother liquor tank is further provided with a backflow port, the backflow port is connected with one end, away from the backflow liquid inlet, of the regulating valve, the backflow port is arranged at the top of the mother liquor tank, and a valve is arranged on a pipeline between the backflow port and the regulating valve.
As optimization, the mother liquor tank is further provided with a liquid level detector, the evaporative crystallization system further comprises a controller, and the liquid level detector and the regulating valve are connected with the controller. The liquid level in the mother liquid tank can be checked by observing the value of the liquid level detector.
Preferably, an electric heating device is arranged on a pipeline between the discharge port and the thickener, and the temperature is controlled to be above 90 ℃. The electric heating device is provided with a heat preservation measure to avoid salt deposition of the discharge pipeline.
The effects provided in the contents of the present invention are only the effects of the embodiments, not all the effects of the present invention, and the above technical solution has the following advantages or advantageous effects:
1. the system can increase the salt yield of the material in unit time and reduce the useless power circulation. The salt deposition of the saturated solution on the inner wall of the pipeline can be effectively avoided, the flow is influenced, and the pipeline blockage is avoided. The salt discharging unit sets linkage control on the continuous salt discharging and discontinuous salt discharging internal reflux systems, and according to the opening degree of the liquid level adjusting valve, the liquidity of the solution in the pipeline is guaranteed, and salt deposition on the inner wall of the pipeline is avoided.
2. The crystallization mixture entering the thickener increases the crystal precipitation amount under the condition of temperature reduction, is particularly obvious for materials with high solubility along with temperature change, and can stir solution by arranging the rotary rake to avoid blocking pipelines.
3. The governing valve can be according to the quantity of backwash liquid with the nimble flow of adjusting of condenser behavior, and sets up at the backwash liquid entrance, can guarantee to be full of liquid in the pipeline, avoids the salt deposition, influences that the pipeline is unobstructed.
4. When the regulating valve is blocked, the valve on the standby pipeline can be opened, and the normal operation of the equipment is prevented from being influenced by emergency treatment. The valves at the front and the rear of the regulating valve can be closed to conveniently replace the regulating valve.
5. Through setting up the mother liquor jar return line, can guarantee the mother liquor jar liquid level, stop the pipeline and block up the problem.
Drawings
FIG. 1 is a schematic diagram of one embodiment of the present invention.
Detailed Description
In order to clearly explain the technical features of the present invention, the following detailed description of the present invention is provided with reference to the accompanying drawings. The following disclosure provides many different embodiments, or examples, for implementing different features of the utility model. To simplify the disclosure of the present invention, the components and arrangements of specific examples are described below. Furthermore, the present invention may repeat reference numerals and/or letters in the various examples. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed. It should be noted that the components illustrated in the figures are not necessarily drawn to scale. Descriptions of well-known components and processing techniques and procedures are omitted so as to not unnecessarily limit the utility model. The terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings for convenience in describing the utility model and for simplicity in description, and do not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be construed as limiting the utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
FIG. 1 shows an embodiment of the present invention, and as shown in the figure, an evaporative crystallization system includes a crystallizer 1, a thickener 2, a centrifuge 3, a mother liquor tank 4, a forced heater 5, a reflux pump 6, a raw material inlet 7, and a circulation pump 8, where the crystallizer 1 is provided with a feed inlet 1.1, a reflux inlet 1.2, a reflux outlet 1.3, and a discharge outlet 1.4, the raw material inlet 7 is connected to the feed inlet 1.1 after passing through the reflux pump 6 and the forced heater 5 in sequence, the reflux outlet 1.3 is connected to the raw material inlet 7, the discharge outlet 1.4 is connected to the thickener 2, the discharge outlet of the thickener 2 is connected to the centrifuge 3, the centrifuge 3 is provided with a mother liquor outlet 3.1 and a salt outlet 3.2, the mother liquor outlet 3.1 is connected to the mother liquor 4, the salt outlet 3.2 is connected to a recovery tank, the bottom of the mother liquor tank 4 is provided with a liquor outlet 4.1, the liquor outlet 4.1 is connected to the reflux inlet 1.2 through the circulation pump 8, a condenser 9 is provided outside the thickener 2, the top of the thickener 2 is provided with a rotary rake 10. The crystallization mixture entering the thickener 2 increases the crystal precipitation amount under the condition of temperature reduction, is particularly obvious for materials with high solubility along with temperature change, and can stir the solution by arranging the rotary rake 10 to avoid blocking pipelines.
The condensing pipe 9 wraps the shell of the thickener 2, the condensing pipe 9 is provided with a cold water inlet and a cold water outlet, the cold water inlet is arranged at the lower part, and the cold water outlet is arranged at the upper part.
The rotary rake 10 comprises a motor and a rake rod, the motor is installed at the top of the thickener 2, the rake rod is connected with an output shaft of the motor, and the rake rod is inserted into the thickener 2.
And a regulating valve 11 is also arranged on a pipeline between the liquid outlet 4.1 and the reflux inlet 1.2.
The regulating valve 11 is located at the reflux inlet 1.2. The regulating valve 11 can flexibly regulate the flow rate according to the quantity of the reflux and the working condition of the condenser, and is arranged at the 1.2 part of the reflux inlet, so that the pipeline can be full of liquid, salt deposition is avoided, and the pipeline is not influenced.
And valves are arranged on the front pipeline and the rear pipeline of the regulating valve 11. The regulating valve 11 can be protected.
And two ends of the regulating valve 11 are also provided with a standby pipeline 12, and the standby pipeline 12 is provided with a valve. When the regulating valve 11 is blocked, the valve on the standby pipeline 12 can be opened for emergency treatment, and the normal operation of the equipment is prevented from being influenced. The regulating valve 11 can be conveniently replaced by closing the valves at the front and the rear of the regulating valve 11.
The mother liquor tank 4 is also provided with a backflow port 4.2, the backflow port 4.2 is connected with one end, away from the backflow inlet 1.2, of the regulating valve 11, the backflow port 4.2 is arranged at the top of the mother liquor tank 4, and a valve is arranged on a pipeline between the backflow port 4.2 and the regulating valve 11. The regulating valve 11 is closed, a valve on a pipeline between the reflux port 4.2 and the regulating valve 11 is opened, and the mother liquor can flow back to the mother liquor tank from the front end of the regulating valve. Under normal conditions, the mother liquor is a major cycle from a liquid outlet 4.1 of the mother liquor tank 4 to the crystallizer through a circulating pump 8, the regulating valve 11 is set for 2min to be opened once, and is opened for 15s once to ensure that the pipeline is smooth, and the opening time is prolonged when the liquid level of the mother liquor tank is high, so that the liquid level of the mother liquor tank is ensured, and the problem of pipeline blockage is avoided.
The mother liquor tank 4 is also provided with a liquid level detector, the evaporative crystallization system further comprises a controller, and the liquid level detector and the regulating valve 11 are connected with the controller. By observing the value of the liquid level detector, the liquid level in the mother liquid tank 4 can be checked. An electric heating device is arranged on a pipeline between the discharge port 1.4 and the thickener 2, and the temperature is controlled to be above 90 ℃. The electric heating device is provided with a heat preservation measure to avoid salt deposition of the discharge pipeline.
The system can increase the salt yield of the material in unit time and reduce the useless power circulation. The salt deposition of the saturated solution on the inner wall of the pipeline can be effectively avoided, the flow is influenced, and the pipeline blockage is avoided. The salt discharging unit sets linkage control on the continuous salt discharging and discontinuous salt discharging internal reflux systems, and according to the opening degree of the liquid level adjusting valve, the liquidity of the solution in the pipeline is guaranteed, and salt deposition on the inner wall of the pipeline is avoided.
Although the present invention has been described with reference to the specific embodiments shown in the drawings, it is not intended to limit the scope of the present invention, and various modifications and variations can be made by those skilled in the art without inventive changes based on the technical solution of the present invention.
Claims (10)
1. An evaporative crystallization system comprises a crystallizer (1), a thickener (2), a centrifugal machine (3), a mother liquor tank (4), a forced heater (5), a reflux pump (6), a raw material inlet (7) and a circulating pump (8), wherein the crystallizer (1) is provided with a feed inlet (1.1), a reflux inlet (1.2), a reflux outlet (1.3) and a discharge outlet (1.4), the raw material inlet (7) is connected with the feed inlet (1.1) after sequentially passing through the reflux pump (6) and the forced heater (5), the reflux outlet (1.3) is connected with the raw material inlet (7), the discharge outlet (1.4) is connected with the thickener (2), the discharge outlet of the thickener (2) is connected with the centrifugal machine (3), the centrifugal machine (3) is provided with a mother liquor outlet (3.1) and a salt outlet (3.2), the mother liquor outlet (3.1) is connected with the mother liquor tank (4), the salt outlet (3.2) is connected with a recovery tank, the bottom of the mother liquor tank (4) is provided with a liquid outlet (4.1), liquid outlet (4.1) is connected reflux entry (1.2) through circulating pump (8), characterized by: a condensing pipe (9) is arranged outside the thickener (2), and a rotary rake (10) is arranged at the top of the thickener (2).
2. An evaporative crystallisation system as claimed in claim 1, wherein the condenser tube (9) encloses the outer shell of the thickener (2), the condenser tube (9) being provided with a cold water inlet and a cold water outlet, the cold water inlet being below and the cold water outlet being above.
3. An evaporative crystallisation system as claimed in claim 1, wherein the rotary rake (10) comprises a motor mounted on top of the thickener (2) and a rake connected to the output shaft of the motor, the rake being inserted into the thickener (2).
4. An evaporative crystallisation system according to claim 1, wherein a regulating valve (11) is provided in the conduit between the liquid outlet (4.1) and the reflux inlet (1.2).
5. An evaporative crystallisation system as claimed in claim 4, wherein said regulating valve (11) is located at the reflux inlet (1.2).
6. An evaporative crystallisation system as claimed in claim 4, wherein valves are provided in both the front and rear lines of the regulating valve (11).
7. An evaporative crystallisation system as claimed in claim 4, wherein the control valve (11) is further provided with a backup line (12) at each end, the backup line (12) being provided with a valve.
8. An evaporative crystallisation system as claimed in claim 4, wherein said mother liquor tank (4) is further provided with a return port (4.2), said return port (4.2) is connected to the end of the regulating valve (11) remote from the return inlet (1.2), said return port (4.2) is arranged at the top of the mother liquor tank (4), and a valve is arranged on the pipeline between the return port (4.2) and the regulating valve (11).
9. The evaporative crystallization system as claimed in claim 4, wherein the mother liquor tank (4) is further provided with a liquid level detector, the evaporative crystallization system further comprises a controller, and the liquid level detector and the regulating valve (11) are connected with the controller.
10. An evaporative crystallisation system as claimed in claim 1, wherein the line between the outlet (1.4) and the thickener (2) is provided with an electrical heating device, the temperature being controlled to above 90 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121538825.0U CN215516706U (en) | 2021-07-07 | 2021-07-07 | Evaporative crystallization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121538825.0U CN215516706U (en) | 2021-07-07 | 2021-07-07 | Evaporative crystallization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215516706U true CN215516706U (en) | 2022-01-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121538825.0U Active CN215516706U (en) | 2021-07-07 | 2021-07-07 | Evaporative crystallization system |
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| Country | Link |
|---|---|
| CN (1) | CN215516706U (en) |
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2021
- 2021-07-07 CN CN202121538825.0U patent/CN215516706U/en active Active
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| Date | Code | Title | Description |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A evaporative crystallization system Granted publication date: 20220114 Pledgee: Overpass Branch of Jinan Rural Commercial Bank Co.,Ltd. Pledgor: SHANDONG BLUESKY ENVIRONMENTAL TECHNOLOGY CO.,LTD. Registration number: Y2024980035972 |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right |