A rotary oxygen generating device and method for a diffuse oxygen supply

Abstract

The application provides a rotary oxygen production device special for diffusion oxygen supply mode, comprising an adsorption bed and a shell, the shell is wrapped outside the adsorption bed, and the shell is internally provided with an adsorption area, a desorption area and a cooling area. The oxygen production mode provided by the application reduces cost and energy consumption, has no noise, is suitable for diffusion oxygen supply mode, and can enrich desorbed nitrogen. The application also desorbs nitrogen by using a vacuum and high-temperature desorption mode, so that the cleaning step in the pressure swing adsorption oxygen production process is omitted, thereby saving oxygen-rich product gas and improving oxygen recovery rate.

Description

Technical Field

[0001] This invention belongs to the field of medical device technology, and specifically relates to a rotary oxygen generator and method for diffusion oxygen supply. Background Technology

[0002] Oxygen is an essential substance for maintaining human life activities and a condition for human survival. Humans depend on oxygen as much as fish cannot live without water. Maintaining the amount of oxygen in the working and living environment is the primary need for human health.

[0003] In industrial applications, commonly used air separation oxygen generation technologies both domestically and internationally include cryogenic distillation, membrane separation, and pressure swing adsorption (PSA). Cryogenic distillation can produce oxygen with a concentration exceeding 99.5%, but it is characterized by high investment, high energy consumption, and complex operation, making it unsuitable for human oxygen supply and widely used in large-scale industrial oxygen production. Membrane separation offers low energy consumption, simple process, and easy operation; however, it only produces oxygen with a concentration of around 40%, and the molecular sieve membranes used in the separation unit are easily damaged and have a limited lifespan, requiring frequent replacement, which indirectly increases the cost of membrane separation and also makes it unsuitable for human oxygen supply. Pressure swing adsorption can produce oxygen with a concentration of around 93%, featuring a simple process, safety, stability, and low cost. Therefore, it is widely used in home oxygen therapy machines and hospital medical oxygen concentrators; however, this process generates significant noise, often disturbing the user's rest.

[0004] With the improvement of people's economic level and the leapfrog progress in medicine, diffusion oxygen supply has become the most common and widely used oxygen supply method due to its simple operation and advantages of being safer and more environmentally friendly. Diffusion oxygen supply is mostly used in rooms, vehicles, wards, mines, and relatively enclosed spaces with dense populations. Especially in high-altitude areas, many hotels use diffusion oxygen supply to prevent discomfort caused by hypoxia in travelers. In addition, diffusion oxygen supply is also frequently used to supply oxygen to construction workers at tunnel faces during the construction of railways and highways in high-altitude areas. The purpose of diffusion oxygen supply is to increase the partial pressure of oxygen in a relatively sealed space to the partial pressure of oxygen outdoors in plains areas, thus making people feel comfortable. Therefore, the oxygen concentration requirements of the oxygen production process are not very high; only a high flow rate of oxygen-enriched product gas, i.e., a high volume or mass of pure oxygen (oxygen concentration of 100%), is needed. Both cryogenic distillation and pressure swing adsorption (PSA) oxygen production processes incur significant costs to enrich air oxygen concentrations to over 90%. However, oxygen diffuses rapidly in the air, meaning the high-concentration oxygen produced is not effectively utilized, resulting in wasted oxygen-enriched product gas and indirectly increasing production costs and energy consumption. Membrane separation oxygen production processes have not achieved widespread application due to the high processing cost and limited lifespan of molecular sieve membranes. In conclusion, current oxygen production processes are not suitable for diffusion-based oxygen supply.

[0005] In view of this, the present invention is hereby proposed. Summary of the Invention

[0006] The purpose of this invention is to provide a rotary oxygen generator and method for diffused oxygen supply. An oxygen-generating adsorbent with nitrogen-oxygen separation properties is loaded onto ceramic fibers and then rolled into a disc shape to form an adsorption bed. When the adsorption bed is in the adsorption zone, it begins to adsorb nitrogen from the incoming air and sends the separated oxygen-enriched product gas to the product gas outlet pipe. When the adsorption bed rotates into the desorption zone, the saturated adsorption bed undergoes desorption and regeneration under high temperature or vacuum conditions in the desorption zone, desorbing and collecting the adsorbed nitrogen. The bed then enters a cooling zone to cool.

[0007] To achieve the above-mentioned technical objectives, the present invention provides the following technical solution:

[0008] The present invention provides a rotary oxygen generator for a diffuse oxygen supply method, comprising an adsorption bed and a shell, the shell covering the outside of the adsorption bed, and the shell having an adsorption zone, a desorption zone and a cooling zone inside, the desorption zone being connected to a vacuum pump for nitrogen removal.

[0009] In existing technologies, pressure swing adsorption (PSA) oxygen generation processes are quite noisy, often affecting the rest of users. Furthermore, when using diffused oxygen supply, the high concentration of oxygen produced by PSA is not effectively utilized, resulting in a waste of oxygen-enriched gas and indirectly increasing oxygen production costs and energy consumption.

[0010] This invention provides a rotary oxygen generator for diffused oxygen supply, comprising a housing with an adsorption zone, a desorption zone, a cooling zone, and an adsorption bed inside. The adsorption bed works in conjunction with the adsorption, desorption, and cooling zones to adsorb and desorb nitrogen gas during rotation. This oxygen generation method reduces cost and energy consumption, and is noiseless, making it suitable for diffused oxygen supply. Furthermore, this invention employs high-temperature and vacuum desorption to desorb nitrogen, eliminating the cleaning step in pressure swing adsorption (PSA) oxygen generation processes, thus saving oxygen-enriched product gas and improving oxygen recovery rate.

[0011] In addition, circumferential baffles are provided on the outside of the adsorption zone, desorption zone, and cooling zone, and a partition plate is provided between the adsorption zone, desorption zone, and cooling zone. The adsorption zone, desorption zone, cooling zone, and circumferential baffles are sealed with sealing material to prevent gas leakage.

[0012] Preferably, the zeolite adsorption bed is an adsorption bed-shaped disc made of rotating ceramic fibers, the cross-section of the ceramic fibers is honeycomb-shaped, and the zeolite adsorption bed is also coated with an oxygen-generating adsorbent.

[0013] Preferably, the oxygen-generating adsorbent is composed of one or more of the following: type A, type X, 3A, 4A, 5A, 13X, Ca-X, Li-X, Ag-X, CaLi-X, AgLi-X, Ca-LSX, Li-LSX, Ag-LSX, CaLi-LSX, AgLi-LSX, MOF, and ZIF.

[0014] Preferably, one side of the adsorption zone is connected to a first air filter, a first compressor, and a first heat exchanger for filtering, compressing, and cooling the air. The other side of the adsorption zone is connected to a pressurized one-way valve, an oxygen storage tank, a product gas outlet pipe, and a first flow control valve for regulating the flow of oxygen-enriched product gas to the cooling zone. The vacuum pump is also connected to a nitrogen storage tank for storing nitrogen. The temperature of the second heat exchanger is 20-40°C higher than the desorption temperature. The heat exchange type can be a shell-and-tube heat exchanger or a regenerative heat exchanger, and the heat exchanger type can be a shell-and-tube heat exchanger, a plate heat exchanger, a jacketed heat exchanger, or an immersed coil heat exchanger, etc.

[0015] Preferably, the product gas outlet pipe is also equipped with an oxygen analyzer to monitor oxygen flow rate and concentration. The oxygen analyzer is connected to a control center system, and the control center system adjusts the oxygen concentration and flow rate based on the data from the oxygen analyzer.

[0016] In addition, the present invention also provides an oxygen generation method using a rotary oxygen generator for diffused oxygen supply, comprising the following steps:

[0017] After the air is filtered, compressed, and cooled, it undergoes adsorption to adsorb nitrogen from the air and outputs oxygen-enriched product gas.

[0018] The adsorption bed rotates to purge and desorb the nitrogen-containing portion, storing some of the desorbed nitrogen and returning the other portion of the desorbed gas to continue purging the adsorption bed.

[0019] The adsorption bed is cooled after desorption.

[0020] Preferably, the flow rate ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas discharged to the application scenario is 0.1:1 to 1:1.

[0021] Preferably, the flow rate ratio of the desorbed gas to the purge air and the nitrogen concentration in the purge gas are related to the purge gas temperature. The lower the purge gas temperature, the lower the flow rate ratio of the desorbed gas to the purge air, and the lower the nitrogen concentration in the purge gas. The flow rate ratio of the desorbed gas to the purge air is 0.1:1 to 1:1, and the nitrogen concentration in the purge gas is 78.08% to 90%.

[0022] Preferably, when the adsorption bed rotates continuously, the adsorption zone, the desorption zone, and the cooling zone occupy the area of ​​the adsorption bed in ratios of 1:4-3:4, 1:8-3:8, and 1:8-3:8, respectively, and the desorption zone and the cooling zone have the same area.

[0023] The adsorption temperature is 5-25℃, the adsorption pressure is 0-50KPa, the desorption temperature is 25-200℃, the pressure in the desorption zone is 0KPa, the rotation speed of the adsorption bed is 3-20r / h, and the air inlet velocity is 0.05-2m / s.

[0024] The temperature of the purge gas is 45-240℃, the flow ratio of the desorbed gas to air in the purge gas is 0.1:1-1:1, the nitrogen concentration in the purge gas is 78.08%-90%, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas provided to the user is 0.1:1-1:1.

[0025] Preferably, when the adsorption bed rotates intermittently, the adsorption zone, the desorption zone, and the cooling zone have the same area.

[0026] The adsorption temperature is 5-25℃, the adsorption pressure is 50-300KPa, the desorption temperature is 25-50℃, the desorption pressure is -100-0KPa, the rotation speed of the adsorption bed is 20-240r / h, the interruption time is 5-60s, the air inlet velocity is 0.05-2m / s, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1-1:1.

[0027] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0028] (1) The present invention can increase the nitrogen adsorption capacity of the adsorbent in the circulating process and improve the oxygen enrichment effect;

[0029] (2) In this invention, an oxygen-generating adsorbent with nitrogen-oxygen separation properties is loaded onto ceramic fibers and then rolled into a disc shape to form an adsorption bed. During the oxygen generation process, the adsorption bed rotates slowly under the drive of a driving device. When the zeolite adsorption bed is in the adsorption zone, it begins to adsorb nitrogen from the incoming air and sends the separated oxygen-enriched product gas to the product gas outlet pipe. When the adsorption bed reaches saturation, it enters the desorption zone. The saturated adsorption bed is desorbed and regenerated under vacuum conditions in the desorption zone to desorb the adsorbed nitrogen, and then enters the cooling zone for cooling. Therefore, this invention has lower noise, reduces the operating energy consumption of the compressor, saves oxygen-enriched product gas, and improves the recovery rate.

[0030] (3) The adsorption oxygen generator of the present invention is easy to operate, has low energy consumption and cost, can continuously generate oxygen-rich product gas and has low noise, and is suitable for use in diffusion oxygen supply. Attached Figure Description

[0031] Various other advantages and benefits will become apparent to those skilled in the art upon reading the following detailed description of preferred embodiments. The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Furthermore, the same reference numerals denote the same parts throughout the drawings. In the drawings:

[0032] Figure 1 This is a schematic diagram of the overall structure of the present invention;

[0033] Figure 2 This is a front view schematic diagram of the zeolite adsorption bed structure of the present invention;

[0034] Figure 3 This is a three-dimensional structural diagram of the zeolite adsorption bed of the present invention;

[0035] Figure 4 This is a three-dimensional structural diagram of the outer shell of the present invention.

[0036] in:

[0037] 1-First air filter; 2-First compressor;

[0038] 3-First heat exchanger; 4-Adsorption zone;

[0039] 5-Pressurized check valve; 6-Oxygen storage tank;

[0040] 7-First flow control valve; 8-Second flow control valve;

[0041] 9-Oxygen filter; 10-Oxygen analyzer;

[0042] 11-Second air filter; 12-Third flow control valve;

[0043] 13-Second compressor; 14-Second heat exchanger;

[0044] 15 - Desorption zone; 16 - Cooling zone;

[0045] 17-Vacuum pump; 18-Fourth flow control valve;

[0046] 19-Fifth flow control valve; 20-Nitrogen storage tank;

[0047] 21- Waste heat pipe; 22- Central control system;

[0048] 23-Sealing material; 24-Adsorption bed;

[0049] 25 - Separator; 26 - Shaft;

[0050] 27-Air intake duct; 28-Product gas outlet duct;

[0051] 29-Purge gas inlet pipe; 30-Desorption pipe;

[0052] 31-Cooling gas inlet pipe; 32-Cooling gas exhaust pipe;

[0053] 33 - Housing; 34 - Mounting bracket;

[0054] 35 - Circumferential baffle; 36 - Rotary shaft hole. Detailed Implementation

[0055] The technical solution of the present invention will be clearly and completely described below with reference to the accompanying drawings and specific embodiments. However, those skilled in the art will understand that the embodiments described below are some embodiments of the present invention, but not all embodiments, and are only used to illustrate the present invention, and should not be regarded as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall be followed. Where the manufacturers of reagents or instruments are not specified, they are all conventional products that can be purchased commercially.

[0056] In the description of this invention, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0057] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0058] To more clearly illustrate the technical solutions in this invention, specific embodiments are described below.

[0059] Example 1

[0060] See Figure 1 The diagram shown is a schematic representation of the overall structure of the present invention. Figure 1 The rotary oxygen generation method can be clearly understood from this.

[0061] First, the air is filtered, pressurized, and cooled by the first air filter, the first compressor, and the first heat exchanger, and then delivered to the adsorption zone to adsorb nitrogen from the air. At this time, the adsorption bed rotates continuously.

[0062] After adsorption, the oxygen-enriched product gas is fed into an oxygen storage tank via a pressurized check valve. The storage tank is equipped with a first flow control valve and a second flow control valve. Opening the first flow control valve allows the oxygen-enriched product gas to enter the cooling zone through a cooling gas inlet pipe to cool the adsorption bed. It then returns to the first compressor through the cooling gas exhaust pipe for pressurization and reuse. Opening the second flow control valve allows the oxygen-enriched product gas to pass through an oxygen filter, and after the oxygen concentration and flow rate are measured by an oxygen analyzer, it can be discharged to the application environment. The oxygen analyzer is connected to a central control system to collect data and adjust the oxygen production flow rate and concentration.

[0063] The third flow control valve opens, allowing air to enter through the second air filter. The air then passes through the second compressor and second heat exchanger on the purge gas inlet pipe before being sent to the desorption zone. The air desorbs the nitrogen adsorbed on the adsorption bed and is then discharged through the desorption pipe. The desorption pipe is connected to a vacuum pump, which maintains a low-pressure vacuum in the desorption zone, facilitating desorption. The nitrogen exiting the vacuum pump and the unreacted air return to the purge gas inlet pipe via the fourth flow control valve and enter the nitrogen storage tank via the fifth flow control valve, respectively.

[0064] The oxygen generating device of the present invention is also surrounded by waste heat pipes, which collect the waste heat emitted from the device and transfer the heat to the second heat exchanger.

[0065] The central control system adjusts the gas flow rate in the first, second, third, fourth, and fifth flow control valves by calculating data from the oxygen analyzer.

[0066] See Figure 2-4 The diagram shown is a structural schematic of the adsorption bed and shell provided by the present invention.

[0067] The oxygen generating device of the present invention includes an adsorption bed and a shell, the shell covering the outside of the adsorption bed. A rotating shaft hole is provided at the center of the adsorption bed for rotation by a rotating shaft, which is connected to a motor to provide power for the rotation of the adsorption bed. The adsorption bed is also coated with an oxygen-generating adsorbent, the composition of which includes type A, type X, 3A, 4A, 5A, 13X, Ca-X, Li-X, Ag-X, CaLi-X, AgLi-X, Ca-LSX, Li-LSX, Ag-LSX, CaLi-LSX, AgLi-LSX, MOF, and ZIF, etc.

[0068] The shell contains an adsorption zone, a desorption zone, and a cooling zone, while the exterior is equipped with circumferential baffles. A partition plate separates the adsorption, desorption, and cooling zones. These zones, along with the circumferential baffles, are sealed with a sealing material to prevent gas leakage. The partition plate separates the adsorption, desorption, and cooling zones, and the adsorption bed works in conjunction with these zones to achieve adsorption, desorption, and cooling during the rotation process.

[0069] An air inlet pipe is located on one side of the adsorption zone of the outer casing, and a product gas outlet pipe is located on the other side of the adsorption zone to supply filtered and compressed air to the adsorption zone. A purge gas inlet pipe is located on the desorption zone of the outer casing, and a desorption pipe is located on the other side of the desorption zone. A cooling gas inlet pipe is located on one side of the cooling zone, and a cooling gas exhaust pipe is located on the other side of the cooling zone. A mounting bracket is also provided on the outer side of the outer casing for easy mounting on an oxygen generator.

[0070] In this embodiment, the ratios of the desorption zone, adsorption zone, and cooling zone to the total area are 3:4, 1:8, and 1:8, respectively. The adsorption temperature is 5℃, the desorption temperature is 200℃, the adsorption pressure is 50 kPa, and the desorption pressure is 0 kPa. The rotational speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1.

[0071] Example 2

[0072] The other operating steps are the same as in Example 1, except that the adsorption bed rotation in this example is intermittent, and the areas of the adsorption zone, desorption zone, and cooling zone are the same. The adsorption temperature is 5℃, the desorption temperature is 30℃, the adsorption pressure is 300KPa, and the desorption pressure is -100KPa. The adsorption bed rotation speed is 60r / h, the rotation interruption time is 20s, the inlet gas flow rate is 0.5m / s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1.

[0073] Example 3

[0074] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the pressure in the adsorption zone is 0 kPa.

[0075] Example 4

[0076] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the pressure in the adsorption zone is 25 kPa.

[0077] Example 5

[0078] Other operating procedures are the same as in Example 1, with a desorption temperature of 200℃, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow rate ratio of the desorbed gas to the purge air is 0.5, and the nitrogen concentration in the purge gas is 82%. The flow rate ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the temperature in the adsorption zone is 25℃.

[0079] Example 6

[0080] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, and an adsorption pressure of 50 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the temperature in the desorption zone is 100°C.

[0081] Example 7

[0082] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the temperature in the desorption zone is 25°C.

[0083] Example 8

[0084] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the rotational speed of the adsorption bed is 3 r / h.

[0085] Example 9

[0086] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the rotational speed of the adsorption bed is 20 r / h.

[0087] Example 10

[0088] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the air inlet flow rate is 0.05 m / s.

[0089] Example 11

[0090] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1, the difference being that the air inlet flow rate is 2 m / s.

[0091] Example 12

[0092] Other operating steps are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas provided to the user is 0.6:1. The difference is that in this example, the ratios of the total area occupied by the desorption zone, adsorption zone, and cooling zone are 1:2, 1:4, and 1:4, respectively.

[0093] Example 13

[0094] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow rate ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the flow rate ratio of the desorbed gas used for purging to the purge air is 0.1:1, and the nitrogen concentration in the purge gas is 78.08%.

[0095] Example 14

[0096] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow rate ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.6:1. The difference is that the flow rate ratio of the desorbed gas used for purging to the purge air is 1:1, and the nitrogen concentration in the purge gas is 90%.

[0097] Example 15

[0098] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The difference is that the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1.

[0099] Example 16

[0100] Other operating procedures are the same as in Example 1, with an adsorption temperature of 5°C, a desorption temperature of 200°C, an adsorption pressure of 50 kPa, and a desorption pressure of 0 kPa. The rotation speed of the adsorption bed is 5 r / h, and the air inlet flow rate is 0.3 m / s. The flow ratio of the desorbed gas to the purge air is 0.5:1, and the nitrogen concentration in the purge gas is 82%. The difference is that the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 1:1.

[0101] Example 17

[0102] The other operating steps are the same as in Example 2, with a desorption temperature of 30°C, an adsorption pressure of 300 kPa, and a desorption pressure of -100 kPa. The adsorption bed rotation speed is 60 r / h, the rotation interruption time is 20 s, the inlet air flow rate is 0.5 m / s, the purge air flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the adsorption temperature is 20°C.

[0103] Example 18

[0104] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, and a desorption pressure of -100 kPa. The adsorption bed rotation speed is 60 r / h, the rotation interruption time is 20 s, the inlet air flow rate is 0.5 m / s, the purge air flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the adsorption pressure is 50 kPa.

[0105] Example 19

[0106] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, and an adsorption pressure of 300 kPa. The adsorption bed rotation speed is 60 r / h, the rotation interruption time is 20 s, the inlet gas flow rate is 0.5 m / s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the desorption pressure is 0 kPa.

[0107] Example 20

[0108] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, an adsorption pressure of 300 kPa, and a desorption pressure of -100 kPa. The inlet gas flow rate is 0.5 m / s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the adsorption bed rotation speed is 20 r / h, i.e., the rotation interruption time is 60 s.

[0109] Example 21

[0110] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, an adsorption pressure of 300 kPa, and a desorption pressure of -100 kPa. The inlet gas flow rate is 0.5 m / s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the adsorption bed rotation speed is 240 r / h, i.e., the rotation interruption time is 5 s.

[0111] Example 22

[0112] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, an adsorption pressure of 300 kPa, and a desorption pressure of -100 kPa. The adsorption bed rotation speed is 60 r / h, the rotation interruption time is 20 s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the air inlet flow rate is 0.05 m / s.

[0113] Example 23

[0114] The other operating steps are the same as in Example 2, with an adsorption temperature of 5°C, a desorption temperature of 30°C, an adsorption pressure of 300 kPa, and a desorption pressure of -100 kPa. The adsorption bed rotation speed is 60 r / h, the rotation interruption time is 20 s, the purge gas flow rate is 0, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1. The difference is that the air inlet flow rate is 2 m / s.

[0115] Example 24

[0116] The other operating steps are the same as in Example 2, wherein the adsorption temperature is 5℃, the desorption temperature is 30℃, the adsorption pressure is 300KPa, and the desorption pressure is -100KPa. The adsorption bed rotation speed is 60r / h, the rotation interruption time is 20s, the inlet air flow rate is 0.5m / s, and the purge air flow rate is 0. The difference is that the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 1:1.

[0117] Based on the above embodiments 1-24, the following data can be obtained:

[0118]

[0119]

[0120] As can be seen from the table above, there is little difference between continuous and intermittent oxygen production methods, and the oxygen production method can be selected according to the applicable scenario.

[0121] As can be seen from the table above, the higher the pressure in the adsorption zone, the higher the oxygen concentration produced.

[0122] As can be seen from the table above, the higher the temperature in the adsorption zone, the lower the oxygen concentration.

[0123] As can be seen from the table above, the faster the rotation speed of the zeolite adsorption bed, the lower the energy consumption.

[0124] As can be seen from the table above, the higher the vacuum pressure in the desorption zone, the greater the oxygen recovery rate.

[0125] As can be seen from the table above, the higher the temperature in the desorption zone, the higher the oxygen concentration and the greater the oxygen recovery rate.

[0126] As can be seen from the table above, the higher the cleaning gas flow rate, the higher the oxygen concentration and the greater the oxygen recovery rate.

[0127] Therefore, it can be concluded that the pressure and temperature of the adsorption zone, the pressure and temperature of the desorption zone, the rotational speed of the zeolite adsorption bed, the flow rate of the cleaning gas, and the area of ​​the adsorption and desorption zones all affect the oxygen concentration, oxygen recovery rate, and energy consumption of this invention. The data in this invention are not derived from simple calculations by those skilled in the art, but rather from data summarized through extensive experiments. This invention merely limits these factors to their optimal range; significant variations in these factors will affect the oxygen production effect of this invention.

[0128] Therefore, it can be concluded that the pressure and temperature of the adsorption zone, the pressure and temperature of the desorption zone, the rotational speed of the zeolite adsorption bed, the flow rate of the cleaning gas, and the area of ​​the adsorption and desorption zones all affect the oxygen concentration, oxygen recovery rate, and energy consumption of this invention. The data in this invention are not derived from simple calculations by those skilled in the art, but rather from data summarized through extensive experiments. This invention merely limits these factors to their optimal range; significant variations in these factors will affect the oxygen production effect of this invention.

[0129] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A rotary oxygen generator for diffused oxygen supply, characterized in that, The device includes an adsorption bed and a shell. The shell covers the outside of the adsorption bed. Inside the shell, there are an adsorption zone, a desorption zone, and a cooling zone. One side of the desorption zone is connected to a vacuum pump for desorbing nitrogen. The other side of the desorption zone is connected to a second air filter, a third flow control valve, a second compressor, and a second heat exchanger. When the third flow control valve is opened, air enters through the second air filter. The air then passes through the second compressor and the second heat exchanger on the purge gas inlet pipe and is sent to the desorption zone. The air desorbs the nitrogen adsorbed on the adsorption bed and is then discharged from the desorption pipe, which is connected to a vacuum pump. This allows the desorption zone to reach a low-pressure vacuum state, which is beneficial for desorption. The nitrogen and unreacted air from the vacuum pump are returned to the purge gas inlet pipe through a fourth flow control valve. The adsorption bed is an adsorption bed-shaped disc made of rotating ceramic fibers. The cross-sectional shape of the ceramic fibers is honeycomb. The adsorption bed is also coated with an oxygen-generating adsorbent. One side of the adsorption zone is connected to a first air filter, a first compressor, and a first heat exchanger for filtering, compressing, and cooling the air. The other side of the adsorption zone is connected to a pressurized one-way valve, an oxygen storage tank, a product gas outlet pipe, and a first flow control valve for regulating the oxygen-enriched product gas delivered to the cooling zone. When the first flow control valve is opened, the oxygen-enriched product gas enters the cooling zone through the cooling gas inlet pipe to cool the adsorption bed. Afterward, it returns to the first compressor through the cooling gas exhaust pipe for pressurization and reuse. The vacuum pump is also connected to a nitrogen storage tank for storing nitrogen gas. An oxygen analyzer is also installed on the product gas outlet pipeline to monitor oxygen flow and concentration. The oxygen analyzer is connected to a control center system, and the control center system adjusts the oxygen concentration and flow based on the data from the oxygen analyzer. The central control system adjusts the gas flow rate in the first, second, third, and fourth flow control valves respectively by calculating the data from the oxygen analyzer.

2. The rotary oxygen generator according to claim 1, characterized in that, The oxygen-generating adsorbent is composed of one or more of the following: type A, type X, MOF, and ZIF.

3. A method for generating oxygen using a rotary oxygen generator for diffused oxygen supply as described in any one of claims 1-2, characterized in that, Includes the following steps: After the air is filtered, compressed, and cooled, it undergoes adsorption to adsorb nitrogen from the air and outputs oxygen-enriched product gas. The adsorption bed rotates to purge and desorb the nitrogen-containing portion, storing some of the desorbed nitrogen and returning the other portion of the desorbed gas to continue purging the adsorption bed. The adsorption bed is cooled after desorption.

4. The oxygen production method according to claim 3, characterized in that, When the adsorption bed rotates continuously, the adsorption zone, the desorption zone, and the cooling zone occupy the area of ​​the adsorption bed in ratios of 1:4-3:4, 1:8-3:8, and 1:8-3:8, respectively, and the desorption zone and the cooling zone have the same area.

5. The oxygen production method according to claim 4, characterized in that, The adsorption temperature is 5-25℃, the adsorption pressure is 0-50KPa, the desorption temperature is 25-200℃, the pressure in the desorption zone is 0KPa, the rotation speed of the adsorption bed is 3-20r / h, and the air inlet velocity is 0.05-2m / s. The temperature of the purge gas is 45-240℃, the flow ratio of desorbed gas to air in the purge gas is 0.1:1-1:1, the nitrogen concentration in the purge gas is 78.08%-90%, and the flow ratio of oxygen-enriched product gas used for cooling to oxygen-enriched product gas provided to users is 0.1:1-1:

1.

6. The oxygen production method according to claim 3, characterized in that, When the adsorption bed rotates intermittently, the adsorption zone, the desorption zone, and the cooling zone have the same area.

7. The oxygen production method according to claim 6, characterized in that, The adsorption temperature is 5-25℃, the adsorption pressure is 50-300KPa, the desorption temperature is 25-50℃, the desorption pressure is -100-0KPa, the rotation speed of the adsorption bed is 20-240r / h, the interruption time is 5-60s, the air inlet velocity is 0.05-2m / s, and the flow ratio of the oxygen-enriched product gas used for cooling to the oxygen-enriched product gas supplied to the user is 0.1:1-1:1.

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