CN116123821A - Starting method of oxygenerator - Google Patents

Starting method of oxygenerator Download PDF

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Publication number
CN116123821A
CN116123821A CN202310161949.9A CN202310161949A CN116123821A CN 116123821 A CN116123821 A CN 116123821A CN 202310161949 A CN202310161949 A CN 202310161949A CN 116123821 A CN116123821 A CN 116123821A
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CN
China
Prior art keywords
tower
liquid
valve
oxygen
air
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Pending
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CN202310161949.9A
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Chinese (zh)
Inventor
祁承钢
曹峥
马吉志
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Angang Steel Co Ltd
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Angang Steel Co Ltd
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Priority to CN202310161949.9A priority Critical patent/CN116123821A/en
Publication of CN116123821A publication Critical patent/CN116123821A/en
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04818—Start-up of the process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention provides an oxygenerator starting method, which comprises the following steps: starting an air compressor and an expander and pressurizing and guiding air in the air separation tower; entering a purification regulating stage, and opening a main cold discharge valve before the liquid oxygen absorber to discharge liquid oxygen-enriched; opening a liquid-air discharge valve of the lower tower to discharge liquid oxygen-enriched in the air separation tower; controlling the gas discharge pressure outside the tower and the oxygen product dispersion amount, and opening a liquid nitrogen regulating valve to a certain position to turn the air separation tower into a normal regulating state; when the oxygen purity of the device rises to a set value A, crude argon is added; when the argon fraction exceeds a preset value B and the pressure of the crude argon tower condenser rises to a preset value C, regulating the pressure of the crude argon tower condenser to D through a flow valve; and the crude argon tower condenser enters a normal working state. The invention adopts the operation method of discharging part of liquid air and liquid oxygen to reduce the main cold liquid level in the cold state starting process of the air separation unit, and can shorten the cold starting time of the unit.

Description

Starting method of oxygenerator
Technical Field
The invention relates to the technical field of energy oxygen, in particular to a starting method of an oxygen generator.
Background
In the prior art, an external compression flow space division device designed by APCI company in the United states is adopted. The starting time of the external compression flow equipment is longer than that of the internal compression flow equipment, the air separation device is started in a cold state, the nitrogen is qualified for 3.5 hours, the oxygen is qualified for 4 hours, and the liquid argon is qualified for 24 hours. Longer starting time and high starting energy consumption.
Disclosure of Invention
According to the technical problems mentioned in the background art, an oxygenerator starting method is provided. The invention mainly utilizes the mode of actively reducing the liquid level to realize the start of the oxygen generator with the product being rapidly qualified.
The invention adopts the following technical means:
an oxygenerator starting method comprises the following steps:
step 1: starting an air compressor and an expander and pressurizing and guiding air in the air separation tower;
step 2: entering a purification regulating stage, and opening a main cold discharge valve before the liquid oxygen absorber to discharge liquid oxygen-enriched;
step 3: opening a liquid-air discharge valve of the lower tower to discharge liquid oxygen-enriched in the air separation tower;
step 4: controlling the gas discharge pressure outside the tower and the oxygen product dispersion amount, and opening a liquid nitrogen regulating valve to a certain position to turn the air separation tower into a normal regulating state;
step 5: when the oxygen purity of the device rises to a set value A, crude argon is added;
step 6: when the argon fraction exceeds a preset value B and the pressure of the crude argon tower condenser rises to a preset value C, regulating the pressure of the crude argon tower condenser to D through a flow valve;
step 7: and the crude argon tower condenser enters a normal working state.
Further, in the step 2, after entering the purification stage, the main cold discharge valve is opened before the liquid oxygen absorber to enable the opening degree of the operation valve to be 30-35%, so that the liquid level of the main condensation evaporator is reduced to 90-95%.
Further, in the step 3, the lower tower liquid air discharge valve is opened to enable the opening degree of the operation valve to be 45-50%, so that the liquid level of the lower tower liquid air is reduced to be 45-50%.
Further, in the step 4, the certain position is that the opening degree of the valve of the nitrogen regulating valve is opened to 41-43%.
Further, the set value a in the step 5 is 95.6-96%.
Further, the preset value B in the step 5 is 30000m 3 /h。
Further, the preset value C is 58-60kPa.
Further, the preset value Dmax does not exceed 70KPa, and the minimum value Dmax cannot be lower than 50KPa.
Compared with the prior art, the invention has the following advantages:
the invention adopts the operation method of discharging part of liquid air and liquid oxygen to reduce the main cold liquid level in the cold state starting process of the air separation unit, and can shorten the cold starting time of the unit. As shown in FIG. 2, oxygen feed in advance, nitrogen feed in advance for 1 hour, and argon feed in advance for 12 hours were realized. The air compressor can perform effective work in advance, saves electric energy, and can produce more products.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to the drawings without inventive effort to a person skilled in the art.
FIG. 1 is a schematic diagram of the whole device of the present invention.
FIG. 2 is a schematic diagram showing the effects of the present invention before and after the implementation.
Detailed Description
In order that those skilled in the art will better understand the present invention, a technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in which it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, shall fall within the scope of the present invention.
It should be noted that the terms "first," "second," and the like in the description and the claims of the present invention and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate such that the embodiments of the invention described herein may be implemented in sequences other than those illustrated or otherwise described herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
As shown in fig. 1, the invention provides a starting method of an oxygenerator, which comprises the following steps:
step 1: starting an air compressor and an expander and pressurizing and guiding air in the air separation tower;
step 2: entering a purification regulating stage, and opening a main cold discharge valve before the liquid oxygen absorber to discharge liquid oxygen-enriched; after entering the purification stage, the main cold discharge valve is opened before the liquid oxygen absorber to enable the opening degree of the operation valve to be 30-35%, so that the liquid level of the main condensation evaporator is reduced to 90-95%. The equipment is an important equipment of the large-scale oxygenerator set, is connected with an upper tower tie and a lower tower tie, and is used for judging whether the working condition is optimal, and whether oxygen and nitrogen products reach standards or not, and sending the oxygen and nitrogen products to a user.
Step 3: opening a liquid-air discharge valve of the lower tower to discharge liquid oxygen-enriched in the air separation tower; opening the liquid-air discharging valve of the lower tower to enable the opening degree of the operating valve to be 45-50%, and enabling the liquid level of the liquid-air of the lower tower to be reduced to 45-50%.
Step 4: controlling the gas discharge pressure outside the tower and the oxygen product dispersion amount, and opening a liquid nitrogen regulating valve to a certain position to turn the air separation tower into a normal regulating state; the certain position is that the opening degree of the valve of the nitrogen regulating valve is opened to 41-43%.
Step 5: when the oxygen purity of the device rises to a set value A, crude argon is added; the set value A is 95.6-96%. The method is characterized in that the oxygen purity in the device starting process is changed from the difference to the oxygen purity in the process, specifically, the main cooling work needs to condense gas nitrogen from a lower tower, and the liquid oxygen from an upper tower is evaporated (the liquid oxygen is evaporated in a main condensation evaporator by utilizing the temperature difference of two substances for heat exchange), namely the purity after the liquid oxygen is evaporated into the gas oxygen. (the gas oxygen evaporated under the condition that the purity of the product is not up to the standard is sent to the outside of the tower to be discharged). Feeding into a crude argon column, wherein the sign is that the pressure of the crude argon column reaches or approaches to the normal value (58-60 KPa) and the liquid-air evaporation capacity gradually reaches 30000m 3 And/h, indicating that the crude argon tower has established rectification to reach a normal working state. The quantity is an important index value for judging the start of the crude argon column.
Step 6: when the argon fraction exceeds a preset value B and the pressure of the crude argon tower condenser rises to a preset value C, regulating the pressure of the crude argon tower condenser to D through a flow valve; the preset value B is 30000m 3 And/h. The preset value C is 58-60kPa. The preset value D is not higher than 70KPa at the highest and cannot be lower than 50KPa.
Step 7: and the crude argon tower condenser enters a normal working state.
The time for qualified delivery of oxygen, nitrogen and argon products to users after the start method of the invention reaches the standard (the shortened time of 2.5 hours for nitrogen, 3.5 hours for oxygen and 12 hours for argon) and the time data which are provided by equipment manufacturers and technical operation rules before the method and are required in actual operation (3.5 hours for nitrogen, 4 hours for oxygen and 24 hours for argon) are respectively the time from the start of the device to the time for qualified delivery of the product purity to a user pipe network after the standard is reached, and the time comparison is clear and obvious.
Example 1
As an embodiment of the application, after the air separation main device is normally started, the method starts to actively reduce the liquid level of the main condensation evaporator and the air separation lower tower after entering the stage of adjusting the purity of the product, artificially changes the reflux ratio in the air separation tower, increases the evaporation of volatile component nitrogen, is beneficial to the separation of oxygen and nitrogen, and shortens the purity qualification time of the individual product.
Step 1: and starting the air compressor, the expander and the air separation tower according to a normal starting operation program, wherein the pressure PI9 of the air separation upper tower is increased to 58-65KPa, and the pressure PI11 of the air separation lower tower is increased to 450-480KPa.
Step 2: and opening a throttling valve of the liquid air removing and separating upper tower of the air separating lower tower to 60-65% of normal opening, and opening a primary cold discharge valve V322-30-35% of the liquid oxygen absorber after entering a purification regulating stage to discharge liquid oxygen enriched. The discharge valve V322 is closed when the main condensing evaporator level LT3 decreases from more than 100% to 90-95% when the vehicle is stopped in the cold state.
And 3, opening a lower tower liquid air discharge valve V270 to 45-50%, and discharging the empty lower tower oxygen-enriched liquid air. When the lower column level LT3 falls to 45-50%, the discharge valve V270 is closed.
Step 4: the given value of the gas discharge regulating PIC79 outside the tower is set to 9.5KPa, the opening of the oxygen diffusing valve FV64 is regulated, the diffusing amount of oxygen products is 25000-27000m3/h, the liquid nitrogen regulating valve HV20 is opened to 41-43%, and the working condition of the main air separation tower is quickly changed into normal.
Step 5: when the oxygen purity AI114 is raised to 95.6-96%, feeding into a crude argon column; the liquid level regulating valve of the crude argon column automatically controls the set value to be 70%, the liquid air reflux valve HV78 of the condenser of the crude argon column is manually opened by 10-12%, and the liquid air reflux valve HV58 of the crude argon column is manually opened by 100%.
Step 6: to an argon fraction of 30000m 3 And (3) when the pressure of the condenser of the crude argon column is increased to 50-55KPa above/h, regulating the pressure of the condenser of the crude argon column to 58-60kPa by using FV-55.
Step 7: the working condition of the crude argon column is quickly changed into normal.
The foregoing embodiment numbers of the present invention are merely for the purpose of description, and do not represent the advantages or disadvantages of the embodiments. In the foregoing embodiments of the present invention, the descriptions of the embodiments are emphasized, and for a portion of this disclosure that is not described in detail in this embodiment, reference is made to the related descriptions of other embodiments. In the several embodiments provided in the present application, it should be understood that the disclosed technology content may be implemented in other manners.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.

Claims (8)

1. The starting method of the oxygenerator is characterized by comprising the following steps of:
step 1: starting an air compressor and an expander and pressurizing and guiding air in the air separation tower;
step 2: entering a purification regulating stage, and opening a main cold discharge valve before the liquid oxygen absorber to discharge liquid oxygen-enriched;
step 3: opening a liquid-air discharge valve of the lower tower to discharge liquid oxygen-enriched in the air separation tower;
step 4: controlling the gas discharge pressure outside the tower and the oxygen product dispersion amount, and opening a liquid nitrogen regulating valve to a certain position to turn the air separation tower into a normal regulating state;
step 5: when the oxygen purity of the device rises to a set value A, crude argon is added;
step 6: when the argon fraction exceeds a preset value B and the pressure of the crude argon tower condenser rises to a preset value C, regulating the pressure of the crude argon tower condenser to D through a flow valve;
step 7: and the crude argon tower condenser enters a normal working state.
2. The method according to claim 1, wherein in step 2, after entering the purification stage, the main cold discharge valve is opened before the liquid oxygen adsorber so that the opening of the operation valve is 30-35%, so that the liquid level of the main condensing evaporator is reduced to 90-95%.
3. The method according to claim 1, wherein in the step 3, the lower tower liquid space discharging valve is opened to open the valve to 45-50%, so that the liquid level of the lower tower liquid space is reduced to 45-50%.
4. The method according to claim 1, wherein in the step 4, the certain position is a position where the opening of the valve of the nitrogen adjusting valve is opened to 41-43%.
5. The method according to claim 1, wherein the set value a in the step 5 is 95.6-96%.
6. The method according to claim 1, wherein the preset value B in the step 5 is 30000m 3 /h。
7. The method of starting an oxygenerator according to claim 1, wherein the preset value C is 58-60kPa.
8. The method according to claim 1, wherein the preset value dmax does not exceed 70KPa and dmin does not fall below 50KPa.
CN202310161949.9A 2023-02-24 2023-02-24 Starting method of oxygenerator Pending CN116123821A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202310161949.9A CN116123821A (en) 2023-02-24 2023-02-24 Starting method of oxygenerator

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202310161949.9A CN116123821A (en) 2023-02-24 2023-02-24 Starting method of oxygenerator

Publications (1)

Publication Number Publication Date
CN116123821A true CN116123821A (en) 2023-05-16

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Family Applications (1)

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CN202310161949.9A Pending CN116123821A (en) 2023-02-24 2023-02-24 Starting method of oxygenerator

Country Status (1)

Country Link
CN (1) CN116123821A (en)

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