CN109761748A - A kind of separation method and device of the synthesising gas systeming carbinol product based on the high division technique of heat - Google Patents
A kind of separation method and device of the synthesising gas systeming carbinol product based on the high division technique of heat Download PDFInfo
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Abstract
The present invention proposes the separation method and device of a kind of synthesising gas systeming carbinol product based on the high division technique of heat, the reaction product of methanol synthesis reactor initially enters middle pressure steam generator and the heat exchange cooling of methanol synthesis reactor input and output material heat exchanger, gas-liquid separation is carried out in high pressure-temperature tank, gas phase enters high pressure low temperature tank after heat exchange is cooling and is further recycled condensation and separation of hydrogen and carbon monoxide, and liquid phase enters low-pressure low-temperature tank after hydraulic turbine is depressured；After the liquid phase of high pressure-temperature knockout drum is depressurized, gas-liquid separation is carried out into low-voltage high-temperature tank, gas phase enters low-pressure low-temperature tank after cooler is cooling, and liquid phase is then methanol product.The present invention is suitable for the gas-liquid separation of synthesising gas systeming carbinol product, in the case where not influencing recycle hydrogen and carbon monoxide purity, methanol yield, it avoids product and direct cools to lower temperature, it can produce steam, and the energy consumption of follow-up process, the more significant cooling load for reducing product separate section are significantly reduced by thermal output.
Description
Technical field
The invention belongs to synthesising gas systeming carbinol technical process methanol synthesis reaction product separation technology fields, in particular to first
The hot high score separation method of alcohol synthetic product separating methanol.
Background technique
For methanol as bulk chemical, the effect in one chemical field of carbon is particularly important.Especially with methanol alkene
The successful development and application of hydrocarbon technique, the dosage of methanol is in being continuously increased.In the process of methanol-fueled CLC, synthesis pressure is 7
Between~10MPa, for reaction temperature between 210~280 DEG C, the product after reacting at this time is gaseous state, in order to isolate methanol,
In production or design, reaction product passes through domestic methanol synthesizer again after being preheated by heat exchanger to synthesis gas at present
Water cooler is cooled to 40 DEG C or so, then carries out gas-liquid separation.In above-mentioned process, have the following problems: (1) methanol reaction tower comes out
Product temperature it is higher, 40 DEG C or so are direct cooled to, wherein cooling load is larger；(2) former process carries out methanol liquid phase
It directly depressurizes, causes the waste of energy.Therefore, it is necessary to develop a kind of work that can reduce cooling load and depressurization energy waste
Skill.
Summary of the invention
In view of the problems of the existing technology, the present invention proposes a kind of synthesising gas systeming carbinol product based on the high division technique of heat
Separation method and device produced using hot high score process methanol-fueled CLC according to the process characteristic of methanol-fueled CLC separate section
Object reduces cooling load and recycles the energy of high pressure liquid phase.
The present invention be solve the problems, such as it is set forth above used by technical solution are as follows:
A kind of device of the synthesising gas systeming carbinol product based on the high division technique of heat, including methanol synthesis reactor input and output material change
Hot device, methanol synthesis reactor, steam generator, high pressure-temperature tank, the first water cooler, high pressure low temperature tank, the first hydraulic turbine,
Low-pressure low-temperature tank, the second hydraulic turbine, low-voltage high-temperature tank, the second water cooler, circulating hydrogen compressor；
Wherein, methanol synthesis reactor input and output material heat exchanger exit is connect with methanol synthesis reactor entrance, methanol-fueled CLC
Reactor outlet is connect with steam generator entrance, steam generator outlet and methanol synthesis reactor input and output material heat exchanger entrance
Connection, methanol synthesis reactor input and output material heat exchanger exit are connect with high-temperature high-pressure tank, high pressure-temperature tank gaseous phase outlet and first
The connection of water cooler entrance, the outlet of the first water cooler are connect with high pressure low temperature tank entrance, high pressure-temperature tank liquid-phase outlet and the second liquid
The connection of power turbine entrance, the outlet of the second hydraulic turbine are connect with low-voltage high-temperature tank；High pressure low temperature tank gaseous phase outlet and recycle hydrogen pressure
The connection of contracting machine entrance, high pressure low temperature tank liquid-phase outlet are connect with the first hydraulic turbine entrance, the outlet of the first hydraulic turbine and low pressure
The connection of cryogenic tank entrance；Low-voltage high-temperature tank gaseous phase outlet is connect with the second water cooler entrance, and the outlet of the second water cooler is low with low pressure
Warm tank entrance connection, low-voltage high-temperature tank liquid-phase outlet are connect with product discharge entrance；Circulating hydrogen compressor outlet and charging
Synthesis gas is connected.
According to the above scheme, the synthesis gas of charging is connect with methanol synthesis reactor input and output material heat exchanger entrance.
According to the above scheme, low-pressure low-temperature tank gaseous phase outlet is connect with torch pipeline, low-pressure low-temperature tank liquid-phase outlet and discharging
Pipeline connection.
The present invention also provides a kind of separation methods of synthesising gas systeming carbinol product, specifically comprise the following steps:
1) pressure is 7~10MPa, and temperature is that 45~65 DEG C of synthesis gas through methanol synthesis reactor input and output material heat exchanger is pre-
It is reacted in methanol synthesis reactor after heat；
2) reaction product in methanol synthesis reactor with successively through steam generator and methanol synthesis reactor input and output material
Heat exchanger is cooled to 85~130 DEG C, and generates 1.0MPa middle pressure steam, into carrying out gas-liquid separation, gas phase in high pressure-temperature tank
Enter high pressure low temperature tank after the first water cooler is cooled to 75~90 DEG C；Liquid phase is depressurized to 0.3 through the second hydraulic turbine~
0.5MPa, into low-voltage high-temperature tank；
3) gas phase of high pressure low temperature tank is recycled through circulating hydrogen compressor compression, and liquid phase is depressurized to through the first hydraulic turbine
0.3~0.5MPa, into low-pressure low-temperature tank；
4) low-voltage high-temperature tank gas phase enters low-pressure low-temperature tank, bottom liquid phases after the second water cooler is cooled to 35~45 DEG C
It is then methanol product；
5) low-pressure low-temperature tank gas phase is incorporated to torch pipeline, and liquid phase is then methanol product.
According to the above scheme, the high pressure-temperature pressure tank is between 7~10MPa, and temperature is between 85~130 DEG C.
According to the above scheme, the high pressure low temperature pressure tank is in 7~10MPa, and temperature is between 75~85 DEG C.
According to the above scheme, the low-voltage high-temperature pressure tank is in 0.3~0.5MPa, and temperature is between 85~130 DEG C.
According to the above scheme, the low-pressure low-temperature pressure tank is in 0.3~0.5MPa, and temperature is between 75~85 DEG C.
Compared with prior art, the invention has the following beneficial effects:
It is directly cold to avoid product in the case where not influencing recycle hydrogen and carbon monoxide purity, methanol yield by the present invention
But lower temperature is arrived, the energy consumption of device follow-up process is significantly reduced, while reducing the cooling load of product separate section, and is produced
Raw 1.0MPa middle pressure steam；Moreover, the energy dissipation caused by avoiding in direct decompression process, has effectively recycled high pressure liquid phase
In energy.
Detailed description of the invention
Fig. 1 is the separation method flow chart of the synthesising gas systeming carbinol product based on the high division technique of heat.
Wherein, 1-methanol synthesis reactor input and output material heat exchanger, 2-methanol synthesis reactors, 3-steam generators, 4-is high
Super pressure-high temperature tank, 5-the first water coolers, 6-high pressure low temperature tanks, 7-the first hydraulic turbines, 8-low-pressure low-temperature tanks, 9-the second fluid power are saturating
It is flat, 10-low-voltage high-temperature tanks, 11-the second water coolers, 12-circulating hydrogen compressors, 13-feed synthesis gas；14-product discharge pipelines；
15-torch pipelines.
Specific embodiment
For a better understanding of the present invention, the content that the present invention is furture elucidated with reference to the accompanying drawings and embodiments, but this
Invention is not limited solely to the following examples.
Embodiment 1
This example is by taking 1,500,000 tons/year of ammonia from coal as an example.As shown in Figure 1, a kind of synthesis gas system based on the high division technique of heat
The device of methanol product, including methanol synthesis reactor input and output material heat exchanger (1), methanol synthesis reactor (2), steam generator
(3), water cooler (5,11), hydraulic turbine (7,9), high pressure-temperature tank (4), high pressure low temperature tank (6), low-voltage high-temperature tank (10), low
Press cryogenic tank (8), circulating hydrogen compressor (12)；
Wherein, the synthesis gas (13) of charging is connect with methanol synthesis reactor input and output material heat exchanger (1) entrance, methanol-fueled CLC
Reactor input and output material heat exchanger (1) outlet connect with methanol synthesis reactor (2) entrance, methanol synthesis reactor (2) export and
The connection of steam generator (3) entrance, steam generator (3) outlet connect with methanol synthesis reactor input and output material heat exchanger (1) entrance
It connects, methanol synthesis reactor input and output material heat exchanger (1) outlet is connect with high-temperature high-pressure tank (4), high pressure-temperature tank (4) gaseous phase outlet
It is connect with the first water cooler (5) entrance, the first water cooler (5) outlet is connect with high pressure low temperature tank (6) entrance, high pressure-temperature tank
(4) liquid-phase outlet is connect with the second hydraulic turbine (9) entrance, the second hydraulic turbine (9) outlet and low-voltage high-temperature tank (10) entrance
Connection；High pressure low temperature tank (6) gaseous phase outlet is connect with circulating hydrogen compressor (12), high pressure low temperature tank (6) liquid-phase outlet and first
The connection of hydraulic turbine (7) entrance, the first hydraulic turbine (7) outlet are connect with low-pressure low-temperature tank (8) entrance；Low-voltage high-temperature tank (10)
Gaseous phase outlet is connect with the second water cooler (11) entrance, and the second water cooler (11) outlet is connect with low-pressure low-temperature tank (8) entrance, low
Super pressure-high temperature tank (10) liquid-phase outlet is connect with discharge pipe (14)；Low-pressure low-temperature tank (8) gaseous phase outlet and torch pipeline (15) are even
It connects, low-pressure low-temperature tank (8) liquid-phase outlet is connect with discharge pipe (14)；Circulating hydrogen compressor (12) outlet and feed synthesis gas
(1) it is connected.
Using above-mentioned apparatus, by taking 1,500,000 tons/year of methanol-fueled CLCs as an example, the method for illustrating separation methanol-fueled CLC product,
Include the following steps:
1) pressure 7MPa, temperature are that 40 DEG C of synthesis gas (13) (composition is shown in Table 1) is changed through methanol synthesis reactor input and output material
It is reacted in methanol synthesis reactor (2) after hot device (1) preheating；
2) reaction product in methanol synthesis reactor (2) is successively and after steam generator (3) and charging heat exchange, temperature drop
To 120 DEG C, and 1.0MPa middle pressure steam is generated, into progress gas-liquid separation, the water cooled device of gas phase (5) in high pressure-temperature tank (4)
Enter high pressure low temperature tank (6) after being cooled to 85 DEG C, further condenses and separates hydrogen and carbon monoxide, the hydrogen separated and an oxidation
Carbon is recycled；The liquid phase of high pressure-temperature tank (4) is depressurized to 0.4MPa through hydraulic turbine (9), into low-voltage high-temperature tank (10) into
Row gas-liquid separation；
3) gas phase of high pressure low temperature tank (6) is recycled through circulating hydrogen compressor (12) compression, and liquid phase is through hydraulic turbine (7)
It is depressurized to 0.4MPa, into low-pressure low-temperature tank (8)；
4) enter low-pressure low-temperature tank (8) after the water cooled device of low-voltage high-temperature tank (10) gas phase (11) is cooled to 40 DEG C and carry out gas-liquid
Separation, bottom liquid phases are then methanol product.
5) low-pressure low-temperature tank (8) gas phase is incorporated to torch pipe network, and liquid phase is then methanol product.
In above-mentioned steps, high pressure-temperature tank (4) pressure is in 7MPa, and temperature is at 120 DEG C；High pressure low temperature tank (6) pressure exists
7MPa, temperature is at 85 DEG C；Low-voltage high-temperature tank (10) pressure is in 0.4MPa, and temperature is at 100 DEG C；Low-pressure low-temperature tank (8) pressure exists
0.4MPa, temperature is at 77 DEG C.
Former traditional process (comparative example 1): synthesis gas is mixed through compressor compresses to 7MPa with circulating air, and gaseous mixture is through passing in and out
Material heat exchanger enters methanol synthesis reactor after being preheated to 240 DEG C；Product after reaction is by input and output material heat exchanger to gaseous mixture
40 DEG C are cooled to through water cooler after preheating；Gas-liquid mixture after cooling enters methanol separator and carries out gas-liquid separation, after separation
Liquid phase enter flash tank, flash tank pressure about 0.5MPa, the liquid phase after flash distillation enters rectification section.
1 embodiment 1 of table is formed with synthesis gas used by comparative example 1
| CO | H2 | CH3OH | CO2 | H2O | |
| Mol% | 28.47 | 67.81 | 0.03 | 2.31 | 0 |
Separation process of the separation method described in the embodiment of the present invention 1 as improved methanol synthesis reaction product, to pass
Separation process of the original process (comparative example 1) of uniting as the methanol synthesis reaction product before transformation, with chemical process simulation software
ASPENPLUS carries out simulation calculating, calculated result such as table 2 and table to the separation process of the methanol synthesis reaction product of transformation front and back
Shown in 3.
In contrast with main group of the transformation of table 2 front and back methanol (mol%)
| CO | H2 | CH3OH | CO2 | H2O | |
| Before transformation | 0.012073 | 0.00469 | 84.6502 | 0.3335 | 14.9995 |
| After transformation | 0.008212 | 0.004424 | 83.7556 | 0.0004527 | 16.2313 |
In contrast with main group of the transformation of table 3 front and back circulating air (mol%)
| CO | H2 | CH3OH | CO2 | H2O | |
| Before transformation | 29.4966 | 68.5875 | 0.5115 | 1.3807 | 0.02369 |
| After transformation | 29.5712 | 66.2565 | 3.972 | 0.007334 | 0.1928 |
The improved separation accuracy of embodiment 1 has variation slightly compared with the separation accuracy before the transformation of comparative example 1, but still
Meet separation requirement, can produce the 1.0MPa steam of 1.3t/h, and cooling load reduces 20%, and high-temperature high-pressure tank is separately recovered
With high pressure low temperature tank liquid phase pressure energy 38KW and 19KW.
Embodiment 2
For this example by taking 1,800,000 tons/year of ammonia from coal as an example, synthesis gas composition is shown in Table 4.Separation methanol-fueled CLC is illustrated to produce
The method of object, includes the following steps:
1) pressure 7MPa, the synthesis gas (13) that temperature is 40 DEG C are preheated through methanol synthesis reactor input and output material heat exchanger (1)
It is reacted in methanol synthesis reactor (2) afterwards；
2) reaction product in methanol synthesis reactor (2) is successively and after steam generator (3) and charging heat exchange, temperature drop
To 120 DEG C, and 1.0MPa middle pressure steam is generated, into progress gas-liquid separation, the water cooled device of gas phase (5) in high pressure-temperature tank (4)
Enter high pressure low temperature tank (6) after being cooled to 85 DEG C, further condenses and separates hydrogen and carbon monoxide, the hydrogen separated and an oxidation
Carbon is recycled；The liquid phase of high pressure-temperature tank (4) is depressurized to 0.4MPa through hydraulic turbine (9), into low-voltage high-temperature tank (10) into
Row gas-liquid separation；
3) gas phase of high pressure low temperature tank (6) is recycled through circulating hydrogen compressor (12) compression, and liquid phase is through hydraulic turbine (7)
It is depressurized to 0.4MPa, into low-pressure low-temperature tank (8)；
4) enter low-pressure low-temperature tank (8) after the water cooled device of low-voltage high-temperature tank (10) gas phase (11) is cooled to 40 DEG C and carry out gas-liquid
Separation, bottom liquid phases are then methanol product.
5) low-pressure low-temperature tank (8) gas phase is incorporated to torch pipe network, and liquid phase is then methanol product.
In above-mentioned steps, high pressure-temperature tank (4) pressure is in 7MPa, and temperature is at 120 DEG C；High pressure low temperature tank (6) pressure exists
7MPa, temperature is at 85 DEG C；Low-voltage high-temperature tank (10) pressure is in 0.4MPa, and temperature is at 100 DEG C；Low-pressure low-temperature tank (8) pressure exists
0.4MPa, temperature is at 80 DEG C.
Former traditional process (comparative example 2): synthesis gas is mixed through compressor compresses to 7MPa with circulating air, and gaseous mixture is through passing in and out
Material heat exchanger enters methanol synthesis reactor after being preheated to 240 DEG C；Product after reaction is by input and output material heat exchanger to gaseous mixture
40 DEG C are cooled to through water cooler after preheating；Gas-liquid mixture after cooling enters methanol separator and carries out gas-liquid separation, after separation
Liquid phase enter flash tank, flash tank pressure about 0.5MPa, the liquid phase after flash distillation enters rectification section.
4 embodiment 2 of table is formed with synthesis gas used by comparative example 2
| CO | H2 | CH3OH | CO2 | H2O | |
| Mol% | 30.67 | 67.91 | 0.03 | 1.31 | 0.08 |
Separation process of the separation method described in the embodiment of the present invention 2 as improved methanol synthesis reaction product, to pass
Separation process of the original process (comparative example 2) of uniting as the methanol synthesis reaction product before transformation, with chemical process simulation software
ASPENPLUS carries out simulation calculating, calculated result such as table 5 and table to the separation process of the methanol synthesis reaction product of transformation front and back
Shown in 6.
In contrast with main group of the transformation of table 5 front and back methanol (mol%)
| CO | H2 | CH3OH | CO2 | H2O | |
| Before transformation | 0.016182 | 0.005643 | 89.2833 | 0.229626 | 10.46519 |
| After transformation | 0.0090654 | 0.004511 | 88.9628 | 0.000748 | 11.022777 |
In contrast with main group of the transformation of table 6 front and back circulating air (mol%)
| CO | H2 | CH3OH | CO2 | H2O | |
| Before transformation | 30.90658 | 67.67802 | 0.5537 | 0.844177 | 0.017456 |
| After transformation | 30.620146 | 65.733652 | 3.5361 | 0.0117923 | 0.098303 |
The improved separation accuracy of embodiment 2 has variation slightly compared with the separation accuracy before the transformation of comparative example 2, but still
Meet separation requirement, can produce the 1.0MPa steam of 1.6t/h, and cooling load reduces 19%, and high-temperature high-pressure tank is separately recovered
With high pressure low temperature tank liquid phase pressure energy 41KW and 20KW.
Therefore, it is straight to avoid product in the case where not influencing recycle hydrogen and carbon monoxide purity, methanol yield by the present invention
It connects and is cooled to lower temperature, significantly reduce the energy consumption of device follow-up process, while reducing the cooling load of product separate section,
And generate 1.0MPa middle pressure steam；Moreover, the energy dissipation caused by avoiding in direct decompression process, has effectively recycled high pressure
Energy in liquid phase.
The above is only a preferred embodiment of the present invention, it is noted that come for those of ordinary skill in the art
It says, without departing from the concept of the premise of the invention, several modifications and variations can also be made, these belong to of the invention
Protection scope.
Claims (8)
1. a kind of separator of the synthesising gas systeming carbinol product based on the high division technique of heat, it is characterised in that anti-including methanol-fueled CLC
Answer device input and output material heat exchanger, methanol synthesis reactor, steam generator, high pressure-temperature tank, the first water cooler, high pressure low temperature tank,
First hydraulic turbine, low-pressure low-temperature tank, the second hydraulic turbine, low-voltage high-temperature tank, the second water cooler, circulating hydrogen compressor；
Wherein, methanol synthesis reactor input and output material heat exchanger exit is connect with methanol synthesis reactor entrance, methanol synthesis reaction
Device outlet is connect with steam generator entrance, and steam generator outlet and methanol synthesis reactor input and output material heat exchanger entrance connect
It connects, methanol synthesis reactor input and output material heat exchanger exit is connect with high-temperature high-pressure tank, high pressure-temperature tank gaseous phase outlet and the first water
The connection of cooler entrance, the outlet of the first water cooler are connect with high pressure low temperature tank entrance, high pressure-temperature tank liquid-phase outlet and the second fluid power
The connection of turbine entrance, the outlet of the second hydraulic turbine are connect with low-voltage high-temperature tank；High pressure low temperature tank gaseous phase outlet and circulation hydrogen compressed
The connection of machine entrance, high pressure low temperature tank liquid-phase outlet are connect with the first hydraulic turbine entrance, and the outlet of the first hydraulic turbine is low with low pressure
Warm tank entrance connection；Low-voltage high-temperature tank gaseous phase outlet is connect with the second water cooler entrance, the outlet of the second water cooler and low-pressure low-temperature
The connection of tank entrance, low-voltage high-temperature tank liquid-phase outlet are connect with product discharge entrance；It is closed with charging circulating hydrogen compressor outlet
It is connected at gas phase.
2. a kind of separator of the synthesising gas systeming carbinol product based on the high division technique of heat, it is characterised in that feed synthesis gas and first
The connection of alcohol synthesis reaction device input and output material heat exchanger entrance.
3. a kind of separator of the synthesising gas systeming carbinol product based on the high division technique of heat, it is characterised in that low-pressure low-temperature tank gas phase
Outlet is connect with torch pipeline, and low-pressure low-temperature tank liquid-phase outlet is connect with product discharge pipeline.
4. a kind of separation method of synthesising gas systeming carbinol product, it is characterised in that include the following steps:
1) pressure is 7~10MPa, after the synthesis gas through methanol synthesis reactor input and output material heat exchanger preheating that temperature is 45~65 DEG C
It is reacted in methanol synthesis reactor；
2) reaction product in methanol synthesis reactor with successively exchange heat through steam generator and methanol synthesis reactor input and output material
Device is cooled to 85~130 DEG C, and generates 1.0MPa middle pressure steam, and into carrying out gas-liquid separation in high pressure-temperature tank, gas phase is through the
One water cooler enters high pressure low temperature tank after being cooled to 75~90 DEG C；Liquid phase is depressurized to 0.3~0.5MPa through the second hydraulic turbine, into
Enter low-voltage high-temperature tank；
3) gas phase of high pressure low temperature tank is recycled through circulating hydrogen compressor compression, and liquid phase is depressurized to 0.3 through the first hydraulic turbine
~0.5MPa, into low-pressure low-temperature tank；
4) low-voltage high-temperature tank gas phase enters low-pressure low-temperature tank after the second water cooler is cooled to 35~45 DEG C, and bottom liquid phases are then
Methanol product；
5) low-pressure low-temperature tank gas phase is incorporated to torch pipe network, and liquid phase is then methanol product.
5. method according to claim 4, it is characterised in that between 7~10MPa, temperature exists the high pressure-temperature pressure tank
Between 85~130 DEG C.
6. method according to claim 4, it is characterised in that the high pressure low temperature pressure tank in 7~10MPa, temperature 75~
Between 85 DEG C.
7. method according to claim 4, it is characterised in that in 0.3~0.5MPa, temperature exists the low-voltage high-temperature pressure tank
Between 85~130 DEG C.
8. method according to claim 4, it is characterised in that in 0.3~0.5MPa, temperature exists the low-pressure low-temperature pressure tank
Between 75~85 DEG C.
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| CN107216236A (en) * | 2017-04-28 | 2017-09-29 | 中石化宁波工程有限公司 | Low pressure methanol synthesis method |
| CN206767964U (en) * | 2017-04-28 | 2017-12-19 | 中石化宁波工程有限公司 | Low pressure methanol synthesis system |
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| CN107216236A (en) * | 2017-04-28 | 2017-09-29 | 中石化宁波工程有限公司 | Low pressure methanol synthesis method |
| CN206767964U (en) * | 2017-04-28 | 2017-12-19 | 中石化宁波工程有限公司 | Low pressure methanol synthesis system |
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Effective date of registration: 20230720 Address after: Room 407, Block B, No. 28, Xinjiekou Outer Street, Xicheng District, Beijing (Desheng Park) Patentee after: BEIJING LANGCLEAN ENVIRONMENT Co.,Ltd. Address before: 230000 floor 1, building 2, phase I, e-commerce Park, Jinggang Road, Shushan Economic Development Zone, Hefei City, Anhui Province Patentee before: Dragon totem Technology (Hefei) Co.,Ltd. Effective date of registration: 20230720 Address after: 230000 floor 1, building 2, phase I, e-commerce Park, Jinggang Road, Shushan Economic Development Zone, Hefei City, Anhui Province Patentee after: Dragon totem Technology (Hefei) Co.,Ltd. Address before: 430081 No. 947 Heping Avenue, Qingshan District, Hubei, Wuhan Patentee before: WUHAN University OF SCIENCE AND TECHNOLOGY |
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