CN111637679A - Liquid oxygen cold energy recovery system and process - Google Patents
Liquid oxygen cold energy recovery system and process Download PDFInfo
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- CN111637679A CN111637679A CN202010394252.2A CN202010394252A CN111637679A CN 111637679 A CN111637679 A CN 111637679A CN 202010394252 A CN202010394252 A CN 202010394252A CN 111637679 A CN111637679 A CN 111637679A
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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
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
- F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine
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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
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D16/00—Devices using a combination of a cooling mode associated with refrigerating machinery with a cooling mode not associated with refrigerating machinery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
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Abstract
The invention provides a liquid oxygen cold energy recovery system and a process, wherein a cold recovery system is connected into an oxygen station, the cold recovery system comprises cold recovery equipment, the cold recovery equipment and an air temperature type vaporizer are connected into a pipe network in parallel, the cold recovery system also comprises a DCS automatic control system, liquid oxygen flows into the cold recovery equipment from a storage tank through a pipeline, the liquid oxygen is vaporized into oxygen after heat exchange with circulating cooling water flowing out of production equipment in the cold recovery equipment, and the circulating cooling water after heat exchange is merged into a circulating cooling water loop of a water chilling unit. The invention recovers the liquid oxygen vaporization cold quantity through the cold recovery device, ensures the reliability and stability of gas supply through the automatic control system, reduces the energy consumption of the water chilling unit, lightens the pressure of the existing cooling loop water system, saves the electric energy, simultaneously improves the stability of gas supply and the product quality, and greatly reduces the frosting of the air temperature vaporizer and the generation of fog.
Description
Technical Field
The invention belongs to the technical field of liquid oxygen cold recovery, and particularly relates to a liquid oxygen cold recovery system and a liquid oxygen cold recovery process.
Background
Liquid oxygen (often abbreviated LOX or LO)2Expressed) is oxygen in liquid stateThe state of the device. It has important application in aerospace, submarine and gas industries. Liquid oxygen is a light blue liquid and has strong paramagnetism. Liquid oxygen has a wide range of industrial and medical uses, with a total expansion ratio of up to 860:1, because of this advantage it is widely used in modern times in industrial production and military applications. Liquid oxygen is generally gasified by a vaporizer in industrial production, and a large amount of cold energy is directly discharged into air and is not recycled in the process of nitrogen rolling gasification. The cold quantity recycling is to recycle cold produced by the vaporization of the liquid oxygen and apply the cold to a refrigeration occasion with certain temperature and display requirements to replace refrigeration equipment and save part of electricity.
The utility model discloses a chinese utility model patent that publication number is CN207163047U discloses a cold volume recycle system of liquid oxygen, including reaction system, official working refrigerating system and production refrigerating system, reaction system includes oxygen therapy pipeline (1) and heat exchange expansion valve (2), and official working refrigerating system and production refrigerating system working medium circulation pass through heat exchange expansion valve (2) respectively, and official working refrigerating system includes equipment room (3) and a plurality of indoor air conditioner (4), and production refrigerating system includes spray set (5), circulating device (6) and heat exchanger (7). When the liquid oxygen gasification device is used, liquid oxygen absorbs a large amount of heat through the heat exchange expansion valve, the office refrigeration system and the production refrigeration system are independently circulated, and working media respectively pass through the heat exchange expansion valve to continuously provide heat for the liquid oxygen gasification process. Office refrigerating system and production refrigerating system working medium circulate to the position of use after reducing, and office refrigerating system can cooperate the fan to cool down the office, and production refrigerating system sprays through the heat transfer and cools down equipment or chemical products to reach the purpose of recycle cold volume. The system simply completes heat exchange of cold energy generated during vaporization of liquid oxygen with an office refrigeration system and a production refrigeration system through a working medium, but the system lacks effective protective measures, safety and reliability cannot be guaranteed, and the problems that the heat exchange quantity is insufficient due to icing inside a heat exchange expansion valve and the temperature of an oxygen outlet is too low easily occur. Therefore, a safe and reliable liquid oxygen refrigeration capacity recovery process is needed to improve refrigeration capacity recovery of liquid oxygen in the using process.
Disclosure of Invention
The invention aims to provide a liquid oxygen cold energy recovery system and a liquid oxygen cold energy recovery process, wherein liquid oxygen vaporization cold energy is recovered through cold recovery equipment, the reliability and stability of gas supply are ensured through an automatic control system, the energy consumption of a water chilling unit is reduced, the pressure of the existing cooling loop water system is reduced, electric energy is saved, the stability of gas supply and the product quality are improved, and the frosting and the mist generation of an air temperature type vaporizer are greatly reduced.
The invention is realized by the following technical scheme:
the invention provides a liquid oxygen cold energy recovery system, which comprises an oxygen station, production equipment and a water chilling unit, wherein the oxygen station consists of a storage tank and an air temperature type vaporizer, a cold recovery component is connected into the oxygen station, the cold recovery component comprises cold recovery equipment, the cold recovery equipment and the air temperature type vaporizer are connected into a pipe network in parallel, the cold recovery assembly further comprises a DCS controller, a first storage tank liquid outlet is connected with the air-temperature vaporizer through a liquid oxygen pipeline, a second storage tank liquid outlet is connected with the cold recovery device through a liquid oxygen pipeline, the air outlets of the air-temperature vaporizer and the cold recovery device are respectively connected with an air inlet of the production device through an oxygen pipeline, a first cooling water outlet of the production device is connected with a water chilling unit through a water pipe, a second cooling water outlet of the production device is connected with the cold recovery device through a two-way water pipe, and a water chilling unit water outlet and a cold recovery device water outlet are connected with a cooling water inlet of the production device through water pipes.
Preferably, the cold recovery apparatus is constituted by a set of double-pipe heat exchangers and a control box.
The invention also provides a liquid oxygen cold energy recovery process, which is characterized by comprising the following steps:
(1) firstly, part of liquid oxygen is sent into an air-temperature vaporizer from a storage tank through a liquid oxygen pipeline, the liquid oxygen is vaporized into oxygen in the air-temperature vaporizer, and the oxygen is conveyed to production equipment through an oxygen pipeline;
(2) the heat generated by the working of the production equipment is absorbed by cooling water, and the cooling water is sent into a water chilling unit through a water pipe to be cooled and then flows back to the production equipment through the water pipe;
(3) and then part of the liquid oxygen is sent into the cold recovery equipment through a liquid oxygen pipeline from the storage tank, meanwhile, a second production equipment cooling water outlet is opened to send cooling water into the cold recovery equipment through a water pipe, the liquid oxygen exchanges heat with the cooling water flowing out of the production equipment in the cold recovery equipment and is vaporized into oxygen, and the cooling water after heat exchange flows back to the production equipment through the water pipe.
Preferably, the total oxygen flow rate in step (1) and step (3) ranges from 100-1500Nm3And h, adjusting the liquid oxygen ratio in the step (1) and the step (3) according to the required oxygen flow and temperature.
Preferably, the volume ratio of liquid oxygen in step (1) and step (3) is 1-3: 1.
Preferably, the oxygen temperature in the step (1) and the oxygen temperature in the step (3) are not lower than-10 ℃, the backwater pressure is not lower than 3bar, and the backwater temperature is not lower than 20 ℃.
Preferably, when the temperature of the oxygen is lower than minus 10 ℃, the two control valves at the liquid outlet of the storage tank are closed, and the liquid oxygen does not flow through the cold recovery equipment and flows through the air-temperature vaporizer completely for vaporization.
Preferably, when the return water temperature is lower than 20 ℃, the two control valves at the liquid outlet of the storage tank are closed, and the liquid oxygen does not flow through the cold recovery equipment and flows through the air-temperature vaporizer completely for vaporization.
Preferably, when the flow rate of the return water is lower than 3bar, the control valve II at the liquid outlet of the storage tank is closed, and the liquid oxygen does not flow through the cold recovery device and flows through the air-temperature vaporizer completely for vaporization.
The invention has the beneficial effects that:
the liquid oxygen cold energy recovery system and the liquid oxygen cold energy recovery process can recover the cold energy of the liquid oxygen used in the production equipment and input the recovered cold energy into the cooling circulating water, thereby reducing the energy consumption of a water chilling unit, reducing the pressure of the existing cooling circulating water system and saving the electric energy.
The liquid oxygen cold energy recovery system and the liquid oxygen cold energy recovery process are controlled by the DCS controller, the oxygen temperature is controlled to be not lower than minus 10 ℃, the return water pressure is not lower than 3bar, the return water temperature is not lower than 20 ℃, insufficient heat exchange quantity caused by icing in the heat exchanger is prevented, stable oxygen supply temperature all the year round can be realized, the gas supply stability and the product quality are improved, and the frosting of the air temperature type vaporizer and the generation of fog are greatly reduced.
Drawings
FIG. 1 is a schematic structural view of a liquid oxygen cold recovery system according to the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments of the present invention and the accompanying drawings, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in figure 1, the invention provides a liquid oxygen cold energy recovery system, which comprises an oxygen station, production equipment and a water chilling unit, wherein the oxygen station consists of a storage tank and an air-temperature vaporizer, a cold recovery assembly is connected into the oxygen station, the cold recovery assembly comprises cold recovery equipment, the cold recovery equipment and the air-temperature vaporizer are connected into a pipe network in parallel, the cold recovery assembly also comprises a DCS controller, a first storage tank liquid outlet is connected with the air-temperature vaporizer through a liquid oxygen pipeline, a second storage tank liquid outlet is connected with the cold recovery equipment through a liquid oxygen pipeline, air outlets of the air-temperature vaporizer and the cold recovery equipment are respectively connected with an air inlet of the production equipment through an oxygen pipeline, a first production equipment cooling water outlet is connected with the water chilling unit through a water pipe, a second production equipment cooling water outlet is connected with the cold recovery equipment through a water pipe, and a water outlet of the water chilling unit and a water outlet of the cold recovery equipment are both connected with a cooling water inlet of, the cold recovery equipment consists of a set of double-sleeve type heat exchanger and a control box.
The invention also provides a liquid oxygen cold energy recovery process, which is characterized by comprising the following steps:
(1) firstly, part of liquid oxygen is sent into an air-temperature vaporizer from a storage tank through a liquid oxygen pipeline, the liquid oxygen is vaporized into oxygen in the air-temperature vaporizer, and the oxygen is conveyed to production equipment through an oxygen pipeline;
(2) the heat generated by the working of the production equipment is absorbed by cooling water, and the cooling water is sent into a water chilling unit through a water pipe to be cooled and then flows back to the production equipment through the water pipe;
(3) and then part of the liquid oxygen is sent into the cold recovery equipment through a liquid oxygen pipeline from the storage tank, meanwhile, a second production equipment cooling water outlet is opened to send cooling water into the cold recovery equipment through a water pipe, the liquid oxygen exchanges heat with the cooling water flowing out of the production equipment in the cold recovery equipment and is vaporized into oxygen, and the cooling water after heat exchange flows back to the production equipment through the water pipe.
The total oxygen flow rate in the steps (1) and (3) is 100-1500Nm3And/h, adjusting the liquid oxygen ratio in the step (1) and the step (3) according to the required oxygen flow and temperature, wherein the volume ratio of the liquid oxygen in the step (1) to the liquid oxygen in the step (3) is 1-3: 1.
And (3) when the temperature of the oxygen is not lower than-10 ℃ and the temperature of the oxygen is lower than-10 ℃, closing the two control valves at the liquid outlet of the storage tank, and completely flowing the liquid oxygen through the air-temperature vaporizer to vaporize without flowing through the cold energy recovery device.
In the step (1) and the step (3), when the return water pressure is not lower than 3bar and the return water flow is lower than 3bar, the two control valves of the liquid outlet of the storage tank are closed, the liquid oxygen does not flow through the cold energy recovery equipment, and the liquid oxygen completely flows through the air temperature type vaporizer to be vaporized
And (3) when the return water temperature is not lower than 20 ℃ and the return water temperature is lower than 20 ℃, closing the second control valve at the liquid outlet of the storage tank, and completely flowing the liquid oxygen through the air-temperature vaporizer to vaporize without flowing through the cold energy recovery device.
Example 1
The liquid oxygen cold energy recovery system and the liquid oxygen cold energy recovery process are used in a certain metal processing plant, and the consumption of the liquid oxygen in the plant is 800Nm3The working time is 24 hours per day, and the gas is stopped for overhauling for 5 days every year, so the liquid oxygen cold energy recovery process data is shown in the following table 1 according to the execution time calculation of 360 days in the whole year:
TABLE 1 liquid oxygen cold recovery process data for metal processing plant
| Item | Symbol | Data of |
| Liquid oxygen consumption (Nm)3/hr) | A | 800 |
| Working time per day (h) | B | 24 |
| Working days per year (d) | C | 360 |
| Liquid oxygen cold energy (Kwh/Nm)3LOX) | D | 0.136 |
| Average electric/cold energy conversion | E | 0.5 |
| Electric charge (Yuan/Kwh) | F | 0.70 |
| CO2Carbon footprint (KgCO)2Degree/degree) | G | 0.566 |
| Circulating water pump power (KW) | H | 0.0 |
| Efficiency of cold recovery plant | J | 85％ |
Energy-saving calculation is performed according to the liquid oxygen cold recovery process data in the table 1, and the obtained data are shown in the table 2:
TABLE 2 liquid oxygen cooling capacity recovery energy-saving data of metal processing plant
| Item | Formula for calculation | Data of |
| Cold energy of liquid oxygen gasification (KW) | K＝A×D×J | 108.8 |
| Electric energy saving quantity (KW) | L＝E×K-H | 46.2 |
| Annual electric charge saving (yuan) | M＝B×C×F×L | 279660 |
| Annual CO2Carbon footprint reduction (ton) | N＝B×C×G×L/1000 | 226 |
This can be seen from Table 2The annual electric charge of the metal processing plant can be saved by about 28 ten thousand yuan, the energy-saving and emission-reduction work is facilitated, the electric load in the plant is reduced, and the annual CO is generated2The emission reduction can reach more than 200 tons, the stable oxygen gas supply temperature all the year around is realized, the stability of gas supply and the product quality are improved, and the risk that the passing in a factory is influenced because a large amount of ice and mist are generated by adopting an air temperature type vaporizer is eliminated.
Example 2
The liquid oxygen cold energy recovery system and the liquid oxygen cold energy recovery process are used in a certain chemical plant, and the consumption of the liquid oxygen in the plant is 300Nm3The working time is 24 hours per day, and the gas is stopped for overhauling for 5 days every year, so the liquid oxygen cold energy recovery process data is shown in the following table 3 according to the execution time calculation of 360 days in the whole year:
TABLE 3 liquid oxygen refrigeration recovery process data of chemical plant
| Item | Symbol | Data of |
| Liquid oxygen consumption (Nm)3/hr) | A | 300 |
| Working time per day (h) | B | 24 |
| Working days per year (d) | C | 360 |
| Liquid oxygen cold energy(Kwh/Nm3LOX) | D | 0.136 |
| Average electric/cold energy conversion | E | 0.5 |
| Electric charge (Yuan/Kwh) | F | 1.2 |
| CO2Carbon footprint (KgCO)2Degree/degree) | G | 0.566 |
| Circulating water pump power (KW) | H | 0.0 |
| Efficiency of cold recovery plant | J | 80％ |
Energy-saving calculation is performed according to the liquid oxygen cold recovery process data in the table 1, and the obtained data are shown in the table 4:
TABLE 4 energy-saving data for recovery of liquid oxygen cold quantity in chemical plant
| Item | Formula for calculation | Data of |
| Cold energy of liquid oxygen gasification (KW) | K＝A×D×J | 32.64 |
| Electric energy saving quantity (KW) | L＝E×K-H | 16.32 |
| Annual electric charge saving (yuan) | M＝B×C×F×L | 169206 |
| Annual CO2Carbon footprint reduction (ton) | N＝B×C×G×L/1000 | 79.8 |
As can be seen from Table 4, the annual electricity charge saving of the chemical plant using the liquid oxygen refrigeration capacity recovery process of the invention can reach about 17 ten thousand yuan, and the annual CO2The emission reduction can reach about 80 tons.
In the description herein, references to the description of "one embodiment," "an example," "a specific example" or the like are intended to mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The preferred embodiments of the invention disclosed above are intended to be illustrative only. The preferred embodiments are not exhaustive or limiting of the specific embodiments of the invention. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best utilize the invention. The invention is limited only by the claims and their full scope and equivalents.
Claims (9)
1. The utility model provides a cold volume recovery system of liquid oxygen, includes oxygen station, production facility and cooling water set, and the oxygen station comprises storage tank and empty warm formula vaporizer, its characterized in that: insert cold recovery subassembly in the oxygen station, cold recovery subassembly includes cold recovery plant, cold recovery plant inserts in the pipe network with the parallelly connected of air temperature formula vaporizer, cold recovery subassembly still includes the DCS controller, storage tank liquid outlet one is connected with air temperature formula vaporizer through the liquid oxygen pipeline, storage tank liquid outlet two is connected with cold recovery plant through the liquid oxygen pipeline, the gas outlet of air temperature formula vaporizer and cold recovery plant is connected with the production facility air inlet through the oxygen pipeline respectively, production facility cooling water delivery port one leads to the pipe and is connected with the cooling water set, production facility cooling water outlet leads to the pipe and is connected with cold recovery plant, cooling water set delivery port and cold recovery plant delivery port all lead to pipe and are connected with production facility cooling water inlet.
2. The liquid oxygen cold recovery system of claim 1, wherein the cold recovery device is composed of a set of double-pipe heat exchanger and a control box.
3. The liquid oxygen cold energy recovery process is characterized by comprising the following steps:
(1) firstly, part of liquid oxygen is sent into an air-temperature vaporizer from a storage tank through a liquid oxygen pipeline, the liquid oxygen is vaporized into oxygen in the air-temperature vaporizer, and the oxygen is conveyed to production equipment through an oxygen pipeline;
(2) the heat generated by the working of the production equipment is absorbed by cooling water, and the cooling water is sent into a water chilling unit through a water pipe to be cooled and then flows back to the production equipment through the water pipe;
(3) and then part of the liquid oxygen is sent into the cold recovery equipment through a liquid oxygen pipeline from the storage tank, meanwhile, a second production equipment cooling water outlet is opened to send cooling water into the cold recovery equipment through a water pipe, the liquid oxygen exchanges heat with the cooling water flowing out of the production equipment in the cold recovery equipment and is vaporized into oxygen, and the cooling water after heat exchange flows back to the production equipment through the water pipe.
4. The liquid oxygen refrigeration capacity recovery process as claimed in claim 3, wherein the total oxygen flow rate in the steps (1) and (3) is in the range of 100-1500Nm3And/h, adjusting the volume ratio of the liquid oxygen in the step (1) and the step (3) according to the required oxygen flow rate and temperature.
5. The liquid oxygen cold recovery process according to claim 4, wherein the volume ratio of the liquid oxygen in the step (1) to the liquid oxygen in the step (3) is 1-3: 1.
6. The liquid oxygen cold energy recovery process according to claim 3, wherein the temperature of oxygen in the step (1) and the temperature of oxygen in the step (3) are not lower than-10 ℃, the pressure of return water is not lower than 3bar, and the temperature of return water is not lower than 20 ℃.
7. The liquid oxygen refrigeration recovery process according to claim 6, wherein the temperature of the oxygen is lower than a set value, an outlet control valve of the refrigeration recovery system is closed, and the liquid oxygen does not flow through the refrigeration recovery heat exchanger and flows through the air temperature type vaporizer to be gasified.
8. The liquid oxygen refrigeration capacity recovery process according to claim 6, wherein the return water temperature is lower than a set value, the outlet control valve of the refrigeration recovery system is closed, and the liquid oxygen does not flow through the refrigeration capacity recovery heat exchanger and flows through the air temperature type vaporizer completely for gasification.
9. The liquid oxygen refrigeration capacity recovery process according to claim 6, wherein the flow rate of the return water is lower than a set value, the outlet control valve of the refrigeration recovery system is closed, and the liquid oxygen does not flow through the refrigeration capacity recovery heat exchanger and flows through the air temperature type vaporizer completely for gasification.
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| CN202010394252.2A CN111637679A (en) | 2020-05-11 | 2020-05-11 | Liquid oxygen cold energy recovery system and process |
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| CN202010394252.2A CN111637679A (en) | 2020-05-11 | 2020-05-11 | Liquid oxygen cold energy recovery system and process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115751183A (en) * | 2022-11-10 | 2023-03-07 | 清远南玻节能新材料有限公司 | Cold and heat quantity circulation exchange energy-saving system and nitrogen making device |
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| CN203534258U (en) * | 2013-11-18 | 2014-04-09 | 上海宝闵工业气体有限公司 | Water tank type device for recycling cold flow of low-temperature liquid products |
| WO2017101775A1 (en) * | 2015-12-16 | 2017-06-22 | 新疆天辰深冷技术有限公司 | Externally-cooled low-purity oxygen air separation system and method |
| CN207163047U (en) * | 2017-07-27 | 2018-03-30 | 苏州吉云新材料技术有限公司 | A kind of liquid oxygen cold recovery utilizes system |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203053140U (en) * | 2013-01-25 | 2013-07-10 | 廊坊黎明气体有限公司 | Recovery device for cold energy produced in liquid air-supply process in air separation system |
| CN203534258U (en) * | 2013-11-18 | 2014-04-09 | 上海宝闵工业气体有限公司 | Water tank type device for recycling cold flow of low-temperature liquid products |
| WO2017101775A1 (en) * | 2015-12-16 | 2017-06-22 | 新疆天辰深冷技术有限公司 | Externally-cooled low-purity oxygen air separation system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115751183A (en) * | 2022-11-10 | 2023-03-07 | 清远南玻节能新材料有限公司 | Cold and heat quantity circulation exchange energy-saving system and nitrogen making device |
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