CN219596290U - SO 2 Equipment for catalytic oxidation of process gas - Google Patents
SO 2 Equipment for catalytic oxidation of process gas Download PDFInfo
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- CN219596290U CN219596290U CN202320420430.3U CN202320420430U CN219596290U CN 219596290 U CN219596290 U CN 219596290U CN 202320420430 U CN202320420430 U CN 202320420430U CN 219596290 U CN219596290 U CN 219596290U
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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
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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Abstract
The utility model discloses an SO 2 The equipment for catalytic oxidation of process gas comprises a combined reactor, wherein the combined reactor comprises a shell, a reaction cavity is arranged in the shell, an air inlet is arranged at the top end of the shell, and an air outlet is arranged at the bottom end of the shell; the combined reactor also comprises a plurality of reactor beds, and the reactor beds are arranged in the reaction cavity and are arranged at intervals along the height direction; the combined reactor also comprises a reactor bed layer arranged between any two adjacent reactor bedsIs provided. SO (SO) 2 Apparatus for catalytic oxidation of process gas for the removal of SO from gas 2 Conversion to SO 3 The utility model not only lays the standard emission of tail gas in the subsequent advanced treatment process, but also further promotes SO while recovering heat by utilizing self reaction heat 2 Is greatly improved in SO 2 The conversion rate of the byproduct steam, the economic benefit and the reasonable energy utilization of the device are realized, the process is simple, the equipment is simple, the device investment is low, and the operation cost is low.
Description
Technical Field
The utility model relates to an SO 2 A device for catalytic oxidation of process gas.
Background
SO 2 Is one of main pollutants in the atmosphere and is also one of important basis for measuring whether the atmosphere is polluted or not. SO (SO) 2 Not only the human health is endangered, the plant growth is endangered, but also acid rain is formed to destroy the ecological environment and public construction, and the corrosion of metal materials and equipment is accelerated. Treatment of SO-containing 2 The process gas desulfurization can not only effectively inhibit environmental pollution, but also can recover sulfur resources to produce finished sulfuric acid to produce economic benefits. Low concentration of SO-containing 2 The desulfurization of process gas solves SO 2 The core of the contamination is located.
SO in the current traditional sulfuric acid production 2 The catalytic oxidation technology has low conversion efficiency, slow reaction speed and SO-containing performance 2 The process gas needs to be dried and contains low concentration SO 2 The wet process gas has poor anti-fluctuation capability, and can not reach the discharge standard and contain SO 2 The stable operation of equipment can be influenced by large fluctuation of process gas, feeding and the like, and the operation is complex, the equipment investment is high, the maintenance cost is high, and the economic benefit can not be generated by effectively recycling the reaction heat byproduct steam generated by the reaction.
Disclosure of Invention
The utility model aims to solve the technical problems of SO in the prior art 2 The catalytic oxidation technology of the process gas has the defects of low conversion efficiency and complex operation, and provides an SO 2 A device for catalytic oxidation of process gas.
The utility model solves the technical problems by the following technical scheme:
SO (SO) device 2 Apparatus for catalytic oxidation of process gas, said apparatus comprising a combined reactor, said combined reactor packageThe device comprises a shell, wherein a reaction cavity is arranged in the shell, an air inlet is arranged at the top end of the shell, and an air outlet is arranged at the bottom end of the shell;
the combined reactor also comprises a plurality of reactor beds, and the reactor beds are arranged in the reaction cavity and are arranged at intervals along the height direction;
the combined reactor further comprises a first heat exchanger arranged between any two adjacent reactor beds.
In this scheme, SO 2 Apparatus for catalytic oxidation of process gas for the removal of SO from gas 2 Conversion to SO 3 The combined reactor is used as a main structure for ensuring the operation of the equipment and comprises a shell and a plurality of reactor beds, wherein the shell is internally provided with a reaction cavity, and the reaction cavity provides a containing space for the reactor beds, SO that the acid process gas can fully react in the reactor beds under the guarantee of the reaction cavity, and SO in the gas is ensured 2 Fully converted into SO 3 The utility model not only lays the standard emission of tail gas in the subsequent advanced treatment process, but also utilizes self reaction heat to recover heat and simultaneously further promotes SO (sulfur dioxide) at the same time 2 Is greatly improved in SO 2 The conversion rate of the byproduct steam, the economic benefit and the reasonable energy utilization of the device are realized, the process is simple, the equipment is simple, the device investment is low, and the operation cost is low.
Preferably, the apparatus comprises a burner, the burner having an inlet and an outlet at each end, the outlet being connected to the air inlet such that the burner and the housing are in communication.
In this scheme, be provided with import and export respectively with the both ends of burning furnace, can make the burning furnace like this can be linked together with the casing, transport the acid process gas after heating to the combined reactor through the export, and the acid process gas just after preheating of initial can get into the burning furnace from the import and carry out the peroxide combustion, accomplishes preliminary desulfurization.
Preferably, the apparatus includes a temperature controller, both ends of which are connected to the outlet and the air inlet, respectively, such that the temperature controller is in communication with the burner and the housing.
In the scheme, the front end of the temperature controller is directly connected with the combustion furnace, and the outlet of the rear end of the temperature controller is connected with the inlet of the combined reactor, so that the temperature controller, the combustion furnace and the combined reactor are communicated, and environmental conditions are provided for the acid process gas to fully perform peroxidation.
Preferably, the apparatus comprises a steam drum, which is connected to the temperature controller.
In the scheme, the steam drum is connected with the temperature controller, and meanwhile, the temperature controller is connected with the combined reactor, so that after the temperature controller exchanges heat with the acid process gas after peroxide combustion in the combustion furnace, heat is recovered, the temperature of the acid process gas is regulated to be suitable for reaction, the acid process gas enters the combined reactor, and the temperature controller sends redundant heat to the steam drum to finish waste heat treatment.
Preferably, the apparatus includes a fan connected to the inlet and in communication with the burner.
In this scheme, the fan is connected in the import, so the fan can be with the acid process gas boost pressure after initially preheating to carry to the burning furnace provides the precondition for fully carrying out the peroxide combustion.
Preferably, the apparatus comprises a steam drum connected to the first heat exchanger.
In this scheme, the steam drum is connected with the first heat exchanger when SO is contained 2 The mixed hot air of the acid process gas enters a combined reactor and SO is carried out under the action of a catalyst 2 Conversion reaction to SO 3 . The reaction process is a strong exothermic reaction, so the first heat exchanger can cool the reaction product to recover heat and is connected with the steam drum, saturated steam generated by the steam drum enters the cold side of the first heat exchanger to further recover heat generated by the acid process gas reaction, and the heat exchange efficiency is improved.
Preferably, the combined reactor comprises a second heat exchanger, wherein the second heat exchanger is positioned at the bottom end in the reaction cavity, and the second heat exchanger is positioned between the air outlet and the reactor bed.
In the scheme, the second heat exchanger is positioned at the bottom end in the reaction cavity, so that hot acid process gas is cooled in the second heat exchanger, the temperature of the acid process gas leaving the second heat exchanger is higher than the dew point temperature, the protection of the inner coating of the sulfuric acid steam condenser and the quartz glass heat exchange tube at the downstream is facilitated, and the thermal shock strength to the coating material and the quartz glass heat exchange tube is reduced.
Preferably, the apparatus comprises a steam drum, which is connected to the second heat exchanger.
In this scheme, the steam pocket is connected with the second heat exchanger, accomplishes the recovery to the heat in the second heat exchanger.
Preferably, a plurality of the reactor beds are provided in three.
In the scheme, the three-bed catalytic reaction can lead SO 2 The conversion rate of the catalyst reaches more than 99 percent. The number of catalytic reaction stages is preferably 3, but can be adjusted according to practical needs. Multiple catalyst beds may achieve better equilibrium conversion.
Preferably, the arrangement comprises a sulfuric acid steam condenser connected to the air outlet.
In the scheme, the sulfuric acid steam condenser is communicated with the air outlet, so that the acid process gas passing through the air outlet is smoothly sent to the sulfuric acid steam condenser for condensation to form acid.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the utility model.
The utility model has the positive progress effects that: in the present utility model, SO 2 Apparatus for catalytic oxidation of process gas for the removal of SO from gas 2 Conversion to SO 3 The combined reactor as the main structure for ensuring the operation of the equipment includes one casing and several reactor beds, and the casing has reaction cavity to provide the reactor bedsThe space ensures that the acid process gas can fully react in the reactor bed layer under the guarantee of the reaction cavity, SO that SO in the gas is reacted 2 Fully converted into SO 3 The utility model not only lays the standard emission of tail gas in the subsequent advanced treatment process, but also utilizes self reaction heat to recover heat and simultaneously further promotes SO (sulfur dioxide) at the same time 2 Is greatly improved in SO 2 The conversion rate of the byproduct steam, the economic benefit and the reasonable energy utilization of the device are realized, the process is simple, the equipment is simple, the device investment is low, and the operation cost is low.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the SO 2 Schematic structural diagram of equipment for catalytic oxidation of process gas.
Reference numerals illustrate:
combined reactor 1
Housing 2
Reaction chamber 21
First heat exchanger 22
Upstream heat exchanger 221
Downstream heat exchanger 222
Second heat exchanger 23
Reactor bed 3
First bed 31
Second bed 32
Third bed 33
Combustion furnace 4
Temperature controller 5
Steam drum 6
Blower 7
Sulfuric acid vapor condenser 8
Detailed Description
The utility model will now be more fully described by way of example only and with reference to the accompanying drawings, but the utility model is not thereby limited to the scope of the examples described.
The embodiment of the utility model discloses an SO 2 Catalytic oxidation device for process gasAs shown in fig. 1, the equipment comprises a combined reactor 1, wherein the combined reactor 1 comprises a shell 2, a reaction cavity 21 is arranged in the shell 2, the top end of the shell 2 is provided with an air inlet, and the bottom end of the shell 2 is provided with an air outlet; the combined reactor 1 further comprises a plurality of reactor beds 3, and the plurality of reactor beds 3 are arranged in the reaction cavity 21 and are arranged at intervals along the height direction; the combined reactor 1 further comprises a first heat exchanger 22 arranged between any adjacent two reactor beds 3. SO (SO) 2 Apparatus for catalytic oxidation of process gas for the removal of SO from gas 2 Conversion to SO 3 The combined reactor 1 is used as a main structure for ensuring the operation of the equipment and comprises a shell 2 and a plurality of reactor beds 3, wherein a reaction cavity 21 is arranged in the shell 2, and the reaction cavity 21 provides a containing space for the reactor beds 3, SO that the acid process gas can fully react in the reactor beds 3 under the guarantee of the reaction cavity 21, and SO in the gas is reacted 2 Fully converted into SO 3 The utility model not only lays the standard emission of tail gas in the subsequent advanced treatment process, but also utilizes self reaction heat to recover heat and simultaneously further promotes SO (sulfur dioxide) at the same time 2 Is greatly improved in SO 2 The conversion rate of the byproduct steam, the economic benefit and the reasonable energy utilization of the device are realized, the process is simple, the equipment is simple, the device investment is low, and the operation cost is low.
Specifically, the wet process acid in this example is carried out by reacting the component SO in the presence of water vapor in the component 2 Catalytic oxidation to SO 3 Thereby further preparing sulfuric acid downstream, solving the problems of high energy consumption and strong corrosion to equipment of a low-concentration sulfur-containing gas device, and the combined reactor 1 is used for preparing SO in low-concentration dust-containing and impurity-containing waste gas 2 Catalytic oxidation to SO 3 (production of H by downstream conversion) 2 SO 4 Is a method of (1). The process overcomes the defects of the prior conventional calcium method and ammonia method desulfurization technology, can achieve higher desulfurization efficiency, has simple process flow, low energy consumption and no secondary pollution, and can produce high-quality sulfuric acid products and byproduct high products at the same timeThe medium-pressure steam in the position not only plays a role in stably promoting SO 2 The effect of conversion reaction realizes the effective utilization of energy and saves the investment of the device.
The device comprises a combustion furnace 4, wherein both ends of the combustion furnace 4 are respectively provided with an inlet and an outlet, and the outlet is directly connected with an air inlet of a temperature controller 5. The air outlet of the temperature controller 5 is connected with the shell 2 of the combined reactor 1, so that the combustion furnace 4 and the shell 2 are communicated. The two ends of the combustion furnace 4 are respectively provided with an inlet and an outlet, so that the combustion furnace 4 can be communicated with the shell 2, the heated acid process gas is conveyed into the combined reactor 1 through the outlet, and the initial acid process gas just preheated can enter the combustion furnace 4 from the inlet to perform peroxidation combustion, so that preliminary desulfurization is completed.
The apparatus includes a temperature controller 5, both ends of the temperature controller 5 are connected to an outlet of the burner 4 and an air inlet of the housing 2 of the combined reactor 1, respectively, such that the temperature controller 5 communicates with the burner 4 and the housing 2. The front end of the temperature controller 5 is directly connected with the combustion furnace 4, and the outlet of the rear end is connected with the inlet of the combined reactor 1, so that the temperature controller 5, the combustion furnace 4 and the combined reactor 1 are communicated, and environmental conditions are provided for the sufficient peroxidation combustion of the acid process gas.
Specifically, the temperature controller 5 includes a heat exchange component, a temperature detection component, a power output component and the like, wherein the temperature detection component detects the temperature of the acid process gas first, the temperature detection component presets a temperature threshold value, and when the high-temperature acid process gas enters, the power output component drives the heat exchange component to cool the acid process gas until the temperature of the acid process gas enters an adaptive temperature range.
Specifically, the drum 6 forms a first waste heat collection circuit with the temperature controller 5.
Specifically, the front-end process of the desulfurization and acid-making process is wet H-containing 2 The acid gas of S is burnt with fuel gas and air to generate SO-containing gas 2 Acid process gas composition fed into combined reactor 1: 4.44% SO 2 ，8.98％O 2 ，10.62％CO 2 ，66.25％N 2 ，8.56％H 2 O, etc. After absorbing heat by the upstream temperature controller 5, part of the hot air is mixed, and the acid process gas reaches the optimal reaction temperature of 390-430 ℃. In this example, the acidic process gas enters the gas inlet at 404 ℃ and is sent to the reactor bed 3 for catalytic oxidation, which is a strongly exothermic reaction.
In the embodiment of the utility model comprising three reactor beds 3, namely a first bed 31, a second bed 32 and a third bed 33, comprising two first heat exchangers 22, namely an upstream heat exchanger 221 and a downstream heat exchanger 222, the acid process gas enters the first bed 31 of the reactor, and the temperature after the reaction is increased to about 507 ℃. The acid process gas from the first bed layer 31 enters the shell side of the upstream first heat exchanger 22 to be cooled and recovered, and is cooled to 410 ℃ after heat exchange with steam produced by equipment. Then the temperature is increased to about 417 ℃ after being sent into the second bed layer 32 for reaction, then the temperature is reduced to 380 ℃ after the heat exchange between the downstream first heat exchanger 22 and the steam produced by the equipment, finally the temperature of the gas after the reaction is about 385 ℃ and the temperature of the acid process gas (285 ℃) leaving the second heat exchanger 23 is about 15-25 ℃ above the dew point temperature of sulfuric acid, so as to prevent the corrosion of the equipment caused by the condensation and deposition of sulfuric acid steam, and simultaneously, the heat impact strength to the coating material and the quartz glass heat exchange pipe is reduced by being beneficial to protecting the inner coating of the downstream sulfuric acid steam condenser 8 and the quartz glass heat exchange pipe. And sending the superheated steam after temperature rising out of the boundary region as a final steam product.
The device comprises a steam drum 6, and the steam drum 6 is connected with a temperature controller 5. The steam drum 6 is connected with the temperature controller 5, and meanwhile, the temperature controller 5 is connected with the combined reactor 1, so that after the temperature controller 5 exchanges heat with the acid process gas after the peroxide combustion in the combustion furnace 4, heat is recovered, the temperature of the acid process gas is regulated to be suitable for reaction, the acid process gas enters the combined reactor 1, and at the moment, the temperature controller 5 sends redundant heat to the steam drum 6 to finish the waste heat collection treatment.
The apparatus comprises a fan 7, the fan 7 being connected to the inlet and being in communication with the combustion air distribution inlet of the combustion furnace 4. The fan 7 is connected to the inlet, so that the fan 7 can boost the pressure of the acid process gas which is preheated initially and convey the acid process gas to the combustion furnace 4, and a precondition is provided for fully performing the peroxygen combustion.
The apparatus comprises a drum 6, the drum 6 being connected to a first heat exchanger 22. The drum 6 is connected to the first heat exchanger 22 when SO-containing 2 The mixed hot air of the acid process gas enters the combined reactor 1 and SO is carried out under the action of the catalyst 2 Conversion reaction to SO 3 . The reaction process is a strong exothermic reaction, so the first heat exchanger 22 can cool down and recover heat, and is connected with the steam drum 6, so that saturated steam generated from the steam drum 6 sequentially enters into the downstream heat exchanger 222 and the upstream heat exchanger 221, and heat generated by the acid process gas reaction is recovered step by step at the cold side, thereby improving heat exchange efficiency.
As shown in fig. 1, specifically, the upstream heat exchanger 221 and the downstream heat exchanger 222 are connected in series, the water fed by the circulating drum 6 in the drum 6 firstly enters the downstream heat exchanger 222 to recover waste heat, the water fed by the circulating drum 6 becomes superheated steam in the process of recovering waste heat, then enters the upstream heat exchanger 221 again to recover waste heat, and the superheated steam after being heated by the upstream heat exchanger 221 is sent out as a final steam product to the boundary zone; the water heater can also be used as a heat source for heating, and is condensed into saturated condensate to be sent out of the shell 2.
The combined reactor 1 comprises a second heat exchanger 23, the second heat exchanger 23 is positioned at the bottom end in the reaction cavity 21, and the second heat exchanger 23 is positioned between the air outlet and the reactor bed 3. The second heat exchanger 23 is positioned at the bottom end in the reaction cavity 21, so that the hot acid process gas is cooled in the second heat exchanger 23, the temperature of the acid process gas leaving the second heat exchanger 23 is higher than the dew point temperature, and meanwhile, the protection of the inner coating of the sulfuric acid steam condenser 8 and the quartz glass heat exchange tube at the downstream is facilitated, and the thermal shock strength to the coating material and the quartz glass heat exchange tube is reduced.
The apparatus comprises a drum 6, the drum 6 being connected to a second heat exchanger 23. The steam drum 6 is connected with the second heat exchanger 23, and the recovery of heat in the second heat exchanger 23 is completed.
Specifically, the cold end of the second heat exchanger 23 feeds water using the recycle drum 6 from the drum 6. Heat exchange of water supply of circulating steam drum 6 and acid process gasThe post vaporization returns to the steam drum 6 to flash to generate the medium pressure saturated steam of 5.0 MPag-5.8 MPag. The acid process gas (SO) exiting the second heat exchanger 23 2 The content is only 0.026%, the conversion rate is more than 99%) and the sulfuric acid is sent to a sulfuric acid steam condenser 8 for condensing to form acid. In which process the SO is gaseous 3 Is combined with water to generate sulfuric acid and condensed to generate 93 to 98 percent of concentrated sulfuric acid. Part of the uncondensed liquid contains a small amount of SO 2 And the acid process gas with a small amount of sulfuric acid is sent to an acid mist catcher, and the tail gas after the tiny mist drops are removed by the acid mist catcher enters a tail gas advanced treatment system. The tail gas advanced treatment system may employ a variety of established wet flue gas desulfurization processes, such as: ammonia desulfurization, calcium desulfurization, double-alkali desulfurization and other new forms of desulfurization.
Specifically, the drum 6 forms a second waste heat collection circuit with the second heat exchanger 23.
The plurality of reactor beds 3 is arranged in three. Three-bed catalytic reaction can lead SO 2 The conversion rate of the catalyst reaches more than 99 percent. The number of catalytic reaction stages is preferably 3, but can be adjusted according to practical needs. Multiple catalyst beds may achieve better equilibrium conversion.
Specifically, a catalyst, SO, is arranged in a reactor coating 2 Conversion of SO 3 The active ingredient of the catalyst is V 2 O 5 。
The device comprises a sulfuric acid steam condenser 8, wherein the sulfuric acid steam condenser 8 is connected with the air outlet. The sulfuric acid steam condenser 8 is communicated with the air outlet, so that the acid process gas passing through the air outlet is smoothly sent into the sulfuric acid steam condenser 8 for condensation to form acid.
While specific embodiments of the utility model have been described above, it will be appreciated by those skilled in the art that this is by way of example only, and the scope of the utility model is defined by the appended claims. Various changes and modifications to these embodiments may be made by those skilled in the art without departing from the principles and spirit of the utility model, but such changes and modifications fall within the scope of the utility model.
Claims (10)
1. SO (SO) device 2 The equipment for catalytic oxidation of the process gas is characterized by comprising a combined reactor, wherein the combined reactor comprises a shell, a reaction cavity is arranged in the shell, an air inlet is formed in the top end of the shell, and an air outlet is formed in the bottom end of the shell;
the combined reactor also comprises a plurality of reactor beds, and the reactor beds are arranged in the reaction cavity and are arranged at intervals along the height direction;
the combined reactor further comprises a first heat exchanger arranged between any two adjacent reactor beds.
2. The SO of claim 1 2 The device for catalytic oxidation of process gas is characterized by comprising a combustion furnace, wherein two ends of the combustion furnace are respectively provided with an inlet and an outlet, and the outlet is connected with the air inlet so that the combustion furnace is communicated with the shell.
3. The SO of claim 2 2 The equipment for catalytic oxidation of process gas is characterized by comprising a temperature controller, wherein two ends of the temperature controller are respectively connected with the outlet and the air inlet, so that the temperature controller is communicated with the combustion furnace and the shell.
4. The SO of claim 3 2 An apparatus for catalytic oxidation of process gas, characterized in that the apparatus comprises a steam drum, which is connected to the temperature controller.
5. The SO of claim 2 2 The equipment for catalytic oxidation of process gas is characterized by comprising a fan, wherein the fan is connected to the inlet and communicated with the combustion furnace.
6. The SO of claim 1 2 An apparatus for the catalytic oxidation of a process gas, characterized in that said apparatus comprises a drum,the steam drum is connected with the first heat exchanger.
7. The SO of claim 1 2 The equipment for catalytic oxidation of the process gas is characterized in that the combined reactor comprises a second heat exchanger, the second heat exchanger is positioned at the bottom end in the reaction cavity, and the second heat exchanger is positioned between the air outlet and the reactor bed.
8. The SO of claim 7 2 The device for catalytic oxidation of process gas is characterized in that the device comprises a steam drum, and the steam drum is connected with the second heat exchanger.
9. The SO of claim 2 2 The equipment for catalytic oxidation of process gas is characterized in that a plurality of reactor beds are arranged in three.
10. The SO of claim 1 2 The equipment for catalytic oxidation of process gas is characterized in that the equipment comprises a sulfuric acid steam condenser, and the sulfuric acid steam condenser is connected with the air outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320420430.3U CN219596290U (en) | 2023-03-07 | 2023-03-07 | SO 2 Equipment for catalytic oxidation of process gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320420430.3U CN219596290U (en) | 2023-03-07 | 2023-03-07 | SO 2 Equipment for catalytic oxidation of process gas |
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| Publication Number | Publication Date |
|---|---|
| CN219596290U true CN219596290U (en) | 2023-08-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320420430.3U Active CN219596290U (en) | 2023-03-07 | 2023-03-07 | SO 2 Equipment for catalytic oxidation of process gas |
Country Status (1)
| Country | Link |
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| CN (1) | CN219596290U (en) |
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2023
- 2023-03-07 CN CN202320420430.3U patent/CN219596290U/en active Active
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