Carbon dioxide in-situ ionization oxygen production device and oxygen preparation method

Abstract

The present invention belongs to the technical field of oxygen production, and specifically relates to a carbon dioxide in-situ ionization oxygen production device and an oxygen production method. The carbon dioxide in-situ ionization oxygen production device includes an air inlet tank and a plasma discharge chamber, wherein the air inlet tank is connected to the plasma discharge chamber, the plasma discharge chamber is connected to an oxygen permeable membrane reactor, a heating jacket is provided on the outside of the oxygen permeable membrane reactor, the oxygen permeable membrane reactor is connected to a gas collecting bottle, and a vacuum pump is connected between the oxygen permeable membrane reactor and the gas collecting bottle; electrodes are provided inside the plasma discharge chamber, a plurality of hollow fiber oxygen permeable membranes are provided inside the oxygen permeable membrane reactor, the plurality of hollow fiber oxygen permeable membranes are fixed on a cluster column, and a vacuum sealing head 1 and a vacuum sealing head 2 are respectively fixed to the left and right ends of the oxygen permeable membrane reactor. The present invention has the advantages of simple equipment structure, easy operation, high efficiency, low energy consumption, high oxygen permeability, and high stability.

Description

Technical Field

[0001] The present invention belongs to the technical field of oxygen preparation, and in particular relates to a carbon dioxide in-situ ionization oxygen production device and an oxygen preparation method. Background Art

[0002] Sending astronauts to Mars has long been a key goal of space exploration. However, the Martian atmosphere is high in CO2, with the remainder consisting of small amounts of N2, argon, and trace amounts of oxygen, water vapor, and ozone, making it difficult for humans to survive. Currently, the most common method for producing oxygen is to use a solid oxide electrolysis cell with scandium oxide and zirconium oxide as the electrolyte to ionize CO2 into CO and O2, but without any O2 purification.

[0003] Chinese patent CN114162787A discloses a CO2 oxygen production device that uses plasma discharge technology to convert CO2 into O2 and CO through a low-temperature plasma reaction. The CO is then removed by adsorption, and the O2 is separated using a precious metal Ag-based oxygen-permeable membrane. However, the Ag-based separation membrane in this process has a low oxygen permeability and is easily corroded by plasma, making it unable to operate stably for a long time, limiting its application.

[0004] Mixed ion-electron perovskite (ABO3) oxygen permeable membrane has attracted widespread attention due to its 100% selectivity for oxygen. However, its poor stability and low oxygen permeability are the main bottlenecks restricting its practical application. 0.5 Sr 0.5 Co 0.3 Fe 0.7 O 3-δ After 5 hours in a CO2 atmosphere, the oxygen permeability of perovskite oxygen permeable membranes is almost halved, making it difficult to match the oxygen production environment on Mars. Analysis of the crystal structure of the perovskite oxygen permeable membrane material shows that it is unstable in a CO2 environment, mainly because the A-site cations react with CO2 to form carbonates that cover their active sites. The high entropy (i.e., configurational entropy greater than 1.5R) strategy will endow the oxygen permeable membrane with the characteristics of slow thermodynamic diffusion, lattice distortion, and a cocktail effect; slow diffusion is beneficial to membrane stability, lattice distortion is conducive to the formation of oxygen vacancies in the titanium oxide oxygen permeable material, and oxygen permeability is increased. The cocktail effect is conducive to improving the CO2 tolerance of the cobalt-based perovskite oxygen permeable material. At the same time, the toughening effect brought by high entropy also provides higher mechanical strength for the hollow fiber membrane.

[0005] Chinese patent CN114904376A discloses a carbon dioxide conversion oxygen production device, which relates to the field of carbon dioxide conversion technology. The carbon dioxide conversion oxygen production device provided by the present invention includes an exhaust assembly, an air intake assembly, a tubular oxygen permeable membrane, a plasma generator and a heating mechanism. The oxygen permeable membrane is installed inside the plasma generator, and a cavity for generating plasma is formed between the oxygen permeable membrane and the plasma generator. The cavity is connected to the air intake assembly, and the interior of the oxygen permeable membrane is connected to the exhaust assembly. The heating mechanism is located outside the plasma generator.

[0006] This patent combines the oxygen permeable membrane with the reaction electrode, which will cause damage to the performance of the oxygen permeable membrane, and the choice of the oxygen permeable membrane will be affected by the combination with the electrode, resulting in lower oxygen permeability and selectivity. Summary of the Invention

[0007] In view of the above deficiencies in the existing technology, the technical problem to be solved by the present invention is: to provide an in-situ carbon dioxide ionization oxygen production device, which can ionize CO2 into O2 and CO under the Martian environment with a high CO2 concentration. The oxygen preparation method provided by the present invention can achieve rapid separation of O2, high CO2 conversion rate, fast O2 separation rate and high purity.

[0008] The technical solution adopted by the present invention to solve its technical problem is:

[0009] The carbon dioxide in-situ ionization oxygen production device described in the present invention includes an air inlet tank and a plasma discharge cabin, the air inlet tank is connected to the plasma discharge cabin, the plasma discharge cabin is connected to an oxygen permeable membrane reactor, a heating jacket is provided on the outside of the oxygen permeable membrane reactor, the oxygen permeable membrane reactor is connected to a gas collecting bottle, and a vacuum pump is connected between the oxygen permeable membrane reactor and the gas collecting bottle; electrodes are provided inside the plasma discharge cabin, the electrodes are connected to a plasma power supply, a plurality of hollow fiber oxygen permeable membranes are provided inside the oxygen permeable membrane reactor, the plurality of hollow fiber oxygen permeable membranes are fixed on a cluster column, and a vacuum sealing head 1 and a vacuum sealing head 2 are respectively fixed at the left and right ends of the oxygen permeable membrane reactor, the vacuum sealing head 1 is connected to the plasma discharge cabin, the vacuum sealing head 2 is connected to the vacuum pump, and the cluster column is connected to the vacuum sealing head 2.

[0010] in:

[0011] The top of the vacuum sealing head 1 is provided with an air inlet hole, the top of the vacuum sealing head 2 is provided with an exhaust hole, the side of the vacuum sealing head 2 is provided with an air outlet hole, and a transmission tube is provided inside the vacuum sealing head 2. One end of the transmission tube is connected to the cluster column, and the other end passes through the air outlet hole to connect to the vacuum pump.

[0012] The tail gas hole is connected with a tail gas bottle.

[0013] A first gas flow meter is connected between the gas inlet tank and the plasma discharge chamber, and a second gas flow meter is connected between the plasma discharge chamber and the oxygen permeable membrane reactor.

[0014] The inner wall of the vacuum sealing head 1, the inner wall of the vacuum sealing head 2 and the outer wall of the oxygen permeable membrane reactor are made of quartz, and the hollow fiber oxygen permeable membrane is made of La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material is prepared with a particle size of 20-60nm, where the particle size is the average particle size; the preparation process includes the following steps:

[0015] a1. Adding a mixture of lanthanum nitrate, calcium nitrate, strontium nitrate, bismuth nitrate, neodymium nitrate, cobalt nitrate and ferric nitrate to deionized water to form a uniform mixed solution B;

[0016] a2. Add ethylene glycol dispersant and citric acid complexing agent to the mixed solution B obtained in step a1, adjust to neutrality with aqueous ammonia, and continue heating and stirring until a gel solution C is formed;

[0017] a3. Heat and dry the gel solution C obtained in step a2 until powdered oxide D is formed;

[0018] a4. After calcining the powdered oxide D obtained in step a3, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ Powder.

[0019] The hollow fiber oxygen permeable membrane is supported by a zinc oxide composite material with through holes formed on the support. The composite material is composed of ZnO-La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ A separation functional layer is set on the outer surface of the support body. The material of the separation functional layer is La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O3-δ The mass ratio of the metal salt in step a1 to the ethylene glycol dispersant and the citric acid complexing agent in step a2 is 1:1-1.5:1; the powdered oxide D in step a4 is calcined at a temperature of 800-1000°C for a calcination time of 4.5-5h. The preparation steps of the hollow fiber oxygen permeable membrane are as follows:

[0020] b1. La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder and ZnO are mixed to obtain mixed powder E;

[0021] b2. Mixing polyethersulfone and N-methylpyrrolidone and stirring until they are completely dissolved to form a transparent solution F;

[0022] b3. Add the mixed powder E to the solution F in batches and continue stirring to form a casting solution G;

[0023] b4. Degas the casting solution G under vacuum, then introduce nitrogen, use N-methylpyrrolidone and ethanol as the core solution and inner coagulation bath, and water as the outer coagulation bath. Driven by pressure, the casting solution is uniformly extruded through a spinneret into the outer coagulation bath, soaked and dried, to obtain the support precursor H;

[0024] b5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder is mixed evenly with 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol and polyvinyl butyral to obtain an impregnation solution I;

[0025] b6. Immersing the support precursor H in the impregnation solution I, then pulling it, and repeating the above pulling process after drying to obtain the hollow fiber precursor J;

[0026] b7. Sinter the hollow fiber precursor J to obtain a hollow fiber oxygen permeable membrane.

[0027] The outer diameter of the through hole of the hollow fiber oxygen permeable membrane is 1.50-1.60 mm, and the thickness of the hollow fiber oxygen permeable membrane is 0.15-0.16 mm; in step b1, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co0.3 Fe 0.7 O 3-δ The mass ratio of powder to ZnO is 7-8:2-3; the mass ratio of polyethersulfone, N-methylpyrrolidone and mixed powder E in step b1 in step b2 is 1:4-5:8; the vacuum degassing time in step b4 is 1-2h, and the nitrogen pressure is 0-0.2MPa; La in step b5 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0. 7O 3-δ The mass ratio of the powder to 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol and polyvinyl butyral is 1:0.8-1.2:1-1.5:0.5-0.8:0.6-0.9:0.5-1:1.2-1.5; the drying temperature in step b6 is 70-90°C; the sintering temperature in step b7 is 1100-1200°C, and the sintering time is 4.5-5.5h.

[0028] The oxygen production method of the carbon dioxide in-situ ionization oxygen production device comprises the following steps:

[0029] S1, pressurizing the CO2 gas in the gas inlet tank and transporting it into the plasma discharge chamber to undergo ionization reaction to obtain ionized gas containing oxygen;

[0030] S2. The ionized gas containing oxygen is transported to the oxygen permeable membrane reactor. Under heating conditions, the ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane. The oxygen enters the interior of the hollow fiber oxygen permeable membrane, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane.

[0031] S3. Collect oxygen into the gas collecting bottle and recover the remaining gas into the tail gas bottle.

[0032] In step S1, the pressure of the CO2-containing gas is 250-350 Pa, the ionization reaction temperature is 180-220° C., the reaction time is 2-5 min, the reaction current is 0.2-0.25 A, and the flow rate of the CO2-containing gas is 50-200 sccm.

[0033] The heating temperature in step S2 is 750-950°C.

[0034] The present invention utilizes an oxygen permeable membrane reactor connected to a plasma discharge chamber to convert CO2 into O2 and separate the O2. With the cooperation of a heating jacket and a vacuum pump, the O2 is extracted from the oxygen permeable membrane reactor, creating a negative pressure inside the reactor. This facilitates the continuous passage of O2 from the ionized gas containing oxygen through the hollow fiber oxygen permeable membrane, resulting in the separation of more oxygen. Multiple hollow fiber oxygen permeable membranes within the oxygen permeable membrane reactor are assembled and fixed by a cluster column. Compared with sheet membranes or single membranes, the effective oxygen permeability area of ​​the oxygen permeable membranes is increased, allowing the ionized O2 to be selectively and continuously output in large quantities through the hollow fiber oxygen permeable membranes. The addition of an external vacuum pump disrupts the chemical reaction equilibrium, allowing the reaction to continuously shift in the positive direction and continuously generate O2. The generated O2 is promptly and effectively output, thereby improving the CO2 conversion rate. The present invention can be used for over 3,000 hours in a CO2 atmosphere.

[0035] The plasma power supply, electrodes, and plasma discharge chamber are collectively referred to as a plasma reaction device, which is connected between the air inlet tank and the oxygen permeable membrane reactor; multiple hollow fiber oxygen permeable membranes are assembled through a bundle column and connected to a vacuum pump through a vacuum sealing head 2 to discharge O2, and an external heating jacket provides energy.

[0036] During use, the gas inlet tank sends the Martian atmosphere gas containing CO2 into the plasma discharge chamber after being detected by a gas flow meter. In the plasma reaction device, the gas is ionized into O2 on the electrode by starting the plasma power supply. The generated mixed gas containing O2 enters the oxygen permeable membrane reactor, and the hollow fiber oxygen permeable membrane selectively separates O2.

[0037] The plasma discharge chamber of the present invention dissociates CO2 into O2 and CO through the action of glow discharge. After dissociation, the mixed gas passes through the hollow fiber membrane to selectively separate O2. Under the high temperature environment of the hollow fiber membrane, O2 absorbs energy and dissociates into oxygen ions on the membrane surface, forming adsorbed oxygen, which then combines with the oxygen vacancies in the perovskite structure to be converted into lattice oxygen. With the oxygen concentration difference on both sides of the membrane as the driving force, the lattice oxygen diffuses from the high concentration end to the low concentration end. At the same time, in order to maintain the electrical neutrality of the membrane, the movement direction of the electrons is opposite to the diffusion direction of the lattice oxygen. When the lattice oxygen diffuses to the low concentration end, it will acquire electrons on the membrane surface and be converted into chemically adsorbed oxygen. The chemically adsorbed oxygen forms oxygen molecules through desorption and leaves the membrane surface in a diffusion manner, thereby achieving the selective separation of O2.

[0038] The beneficial effects of the present invention are:

[0039] The present invention ionizes CO2 in situ and then uses high entropy perovskite La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3Fe 0. 7O 3-δ The material separates ionized CO and O2 without adsorption to achieve high-purity oxygen purification, thereby improving its oxygen permeability, CO2 tolerance and long-term stability to meet practical applications in the Martian environment.

[0040] When the CO2 in-situ ionization oxygen generator is operating, a Martian atmosphere gas mixture containing CO2 from a gas inlet tank is first fed into the plasma discharge chamber. At the electrodes of the plasma reactor, the CO2 is ionized into O2 and CO by a power source. The CO2 is then fed into the oxygen permeable membrane reactor. The heating jacket is activated, and at a certain temperature, the hollow fiber oxygen permeable membrane selectively separates the O2-containing gas mixture. A vacuum pump then extracts the O2, increasing the oxygen partial pressure on both sides of the hollow fiber oxygen permeable membrane, thereby accelerating the O2 entry and separation rate. The O2 concentration gradient on both sides of the hollow fiber oxygen permeable membrane acts as the driving force, causing oxygen molecules to diffuse from the high-oxygen end to the low-oxygen end, resulting in higher-purity O2.

[0041] The present invention combines plasma ionization to produce O2 with an oxygen-permeable membrane reactor to separate O2, offering advantages such as simple equipment, easy operation, high efficiency, and low energy consumption. The in-situ carbon dioxide ionization oxygen production device combines a plasma reactor with an oxygen-permeable membrane reactor to ionize CO2 into O2 and CO, and selectively separate O2, with simple operation.

[0042] The oxygen permeable membrane material adopts a multi-cation doping strategy to achieve high entropy perovskite La with high oxygen flux and CO2 resistance. 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The present invention doped Ca at the A position 2+ 、Bi 3+ and Nd 3+ High-valent cations such as cations will increase oxygen vacancies and surface reaction rates, thereby increasing oxygen ion conductivity and oxygen permeability; due to the weak alkalinity of the doped cations and the enhancement of the AO bond energy, it is more difficult for them to combine with CO2, thus effectively increasing the La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ Stability; Ca 2+ 、Bi 3+ and Nd 3+The multi-cation doping and the ratio between the various components make the material have high entropy characteristics; its A-site configuration entropy is 1.56R, with the characteristics of slow diffusion, severe lattice distortion and cocktail effect. Lattice distortion is conducive to the formation of oxygen vacancies in titanium oxide oxygen permeable materials. The cocktail effect improves the CO2 tolerance of Co-containing perovskite oxygen permeable materials. At the same time, the toughening effect brought by high entropy also provides higher mechanical strength for the hollow fiber membrane; its tolerance factor is 0.859, which meets the regulation of perovskite structure stability. Compared with other compositions, such as La 0.2 Ca 0.2 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ、 La 0.2 Ca 0.2 Sr 0.3 Bi 0.1 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ Wait, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ It has high oxygen permeability and stability.

[0043] The oxygen permeable membrane is hollow fiber type and the oxygen separation process is in a negative pressure state, which can simultaneously maximize the reaction surface area, maximize the oxygen permeation driving force, and minimize the resistance. It can also operate stably in an acidic atmosphere for a long time while ensuring the oxygen permeability. BRIEF DESCRIPTION OF THE DRAWINGS

[0044] Figure 1 It is a schematic structural diagram of the present invention;

[0045] Figure 2 Schematic diagram of the structure of the oxygen permeable membrane reactor of the present invention;

[0046] Figure 3 This is a structural schematic diagram of a vacuum sealing head according to the present invention;

[0047] Figure 4 This is a schematic diagram of the second structure of the vacuum sealing head of the present invention;

[0048] Figure 5 This is a side view of the second structure of the vacuum sealing head of the present invention;

[0049] Figure 6 Schematic diagram of the cluster column structure of the present invention;

[0050] Figure 7 This is a left view of the cluster column structure of the present invention;

[0051] Figure 8 This is a right view of the cluster column structure of the present invention;

[0052] Figure 9 Schematic diagram of the structure of the hollow fiber oxygen permeable membrane in Example 1 of the present invention;

[0053] Figure 10 is a SEM image of the hollow fiber oxygen permeable membrane of Example 1 of the present invention at 500 μm;

[0054] Figure 11 This is a SEM image of the hollow fiber oxygen permeable membrane of Example 1 of the present invention at 50 μm;

[0055] Figure 12 is a SEM image of the hollow fiber oxygen permeable membrane of Example 1 of the present invention at 100 μm;

[0056] Figure 13 This is a SEM image of the hollow fiber oxygen permeable membrane of Example 1 of the present invention at 20 μm;

[0057] Figure 14 This is a graph showing the detection data of carbon dioxide content in the gas collecting bottles of Examples 1-5 of the present invention;

[0058] Figure 15 This is a graph showing the carbon monoxide content detection data in the gas collecting bottles of Examples 1-5 of the present invention;

[0059] Figure 16 This is a graph showing the nitrogen content detection data in the gas collecting bottles of Examples 1-5 of the present invention;

[0060] Figure 17 1 is a graph showing the oxygen content detection data in the gas collecting bottle of Examples 1-5 of the present invention;

[0061] Figure 18 This is a TEM image of the hollow fiber oxygen permeable membrane material prepared in Example 1 of the present invention;

[0062] Figure 19 This is a stability data chart of the hollow fiber oxygen permeable membrane prepared in Example 1 of the present invention after being purged with CO2 purge gas;

[0063] In the figure: 1. Gas inlet tank; 2. Plasma discharge chamber; 3. Oxygen permeable membrane reactor; 4. Heating jacket; 5. Gas collecting bottle; 6. Vacuum pump; 7. Tail gas bottle; 101. Gas flow meter 1; 201. Plasma power supply; 202. Electrode; 203. Gas flow meter 2; 301. Hollow fiber oxygen permeable membrane; 302. Cluster column; 303. Vacuum sealing head 1; 304. Vacuum sealing head 2; 3031. Gas inlet hole; 3041. Tail gas hole; 3042. Gas outlet hole; 3043. Transmission pipe. DETAILED DESCRIPTION

[0064] The embodiments of the present invention will be further described below with reference to the accompanying drawings.

[0065] Example 1

[0066] like Figure 1-9 As shown, the carbon dioxide in-situ ionization oxygen production device described in the present invention includes an air inlet tank 1 and a plasma discharge cabin 2, the air inlet tank 1 is connected to the plasma discharge cabin 2, the plasma discharge cabin 2 is connected to an oxygen permeable membrane reactor 3, a heating jacket 4 is provided on the outside of the oxygen permeable membrane reactor 3, the oxygen permeable membrane reactor 3 is connected to a gas collecting bottle 5, and a vacuum pump 6 is connected between the oxygen permeable membrane reactor 3 and the gas collecting bottle 5; an electrode 202 is provided inside the plasma discharge cabin 2, the electrode 202 is connected to a plasma power supply 201, a plurality of hollow fiber oxygen permeable membranes 301 are provided inside the oxygen permeable membrane reactor 3, the plurality of hollow fiber oxygen permeable membranes 301 are fixed on a cluster column 302, and a vacuum sealing head 1 303 and a vacuum sealing head 2 304 are fixed on the left and right ends of the oxygen permeable membrane reactor 3 respectively, the vacuum sealing head 1 303 is connected to the plasma discharge cabin 2, the vacuum sealing head 2 304 is connected to the vacuum pump 6, and the cluster column 302 is connected to the vacuum sealing head 2 304.

[0067] An air inlet 3031 is provided at the top of the vacuum sealing head 1 303, an exhaust hole 3041 is provided at the top of the vacuum sealing head 2 304, an air outlet 3042 is provided on the side of the vacuum sealing head 2 304, and a transmission tube 3043 is provided inside the vacuum sealing head 2 304. One end of the transmission tube 3043 is connected to the cluster column 302, and the other end passes through the air outlet 3042 to connect to the vacuum pump 6.

[0068] The tail gas hole 3041 is connected to the tail gas bottle 7 .

[0069] A gas flow meter 101 is connected between the gas inlet tank 1 and the plasma discharge chamber 2 , and a gas flow meter 203 is connected between the plasma discharge chamber 2 and the oxygen permeable membrane reactor 3 .

[0070] The inner wall of the vacuum sealing head 1 303, the inner wall of the vacuum sealing head 2 304 and the outer wall of the oxygen permeable membrane reactor 3 are made of quartz, and the hollow fiber oxygen permeable membrane 301 is made of La 0.3 Ca 0.1 Sr0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material is prepared with a particle size of 20nm; the preparation process includes the following steps:

[0071] a1. Add 100 g of a mixture of lanthanum nitrate, calcium nitrate, strontium nitrate, bismuth nitrate, neodymium nitrate, cobalt nitrate, and ferric nitrate to deionized water to form a uniform mixed solution B.

[0072] a2. Add 150 g of ethylene glycol dispersant and 100 g of citric acid complexing agent to the mixed solution B obtained in step a1, then add ammonia water to adjust the pH to neutral, and continue heating and stirring until a gel solution C is formed;

[0073] a3. Heat and dry the solution C obtained in step a2 until powdered oxide D is formed;

[0074] a4. Calcine the oxide D obtained in step a3 at 800°C for 5 hours to obtain La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ powder;

[0075] Hollow fiber oxygen permeable membrane 301 is composed of ZnO-La composite material 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The composite material is a support body, a through hole is provided on the support body, and a separation functional layer is provided on the outer surface of the support body. The material of the separation functional layer is La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The preparation steps of the hollow fiber oxygen permeable membrane 301 are as follows:

[0076] b1. La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe0.7 O 3-δ The powder and ZnO were mixed in a mass ratio of 7:3 to obtain 80 g of mixed powder E;

[0077] b2. Mix 10 g of polyethersulfone and 40 g of N-methylpyrrolidone and stir until they are completely dissolved to form a light yellow transparent solution F;

[0078] b3. Add the mixed powder E to the solution F in batches and continue stirring to form a casting solution G;

[0079] b4. Degas the casting liquid G under vacuum for 1.5 h, then introduce nitrogen at a pressure of 0.1 MPa. Use N-methylpyrrolidone and ethanol as the core liquid and inner coagulation bath, and water as the outer coagulation bath. Driven by pressure, the casting liquid is uniformly extruded through the spinneret into the outer coagulation bath, soaked and dried, to obtain the support body precursor H;

[0080] b5. According to the mass ratio of 1:0.8:1.5:0.5:0.8:0.7:1.5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder, 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol and polyvinyl butyral are added to a planetary ball mill and mixed evenly to obtain an impregnation solution I;

[0081] b6. Immerse the support precursor H in the impregnation solution I, then pull it, dry it at 80°C, and repeat the above pulling process to obtain the hollow fiber precursor J;

[0082] b7. Sinter the hollow fiber precursor J at 1200° C. for 5 h to obtain the hollow fiber oxygen permeable membrane 301 ; the outer diameter of the through hole of the hollow fiber oxygen permeable membrane 301 is 1.50 mm, and the thickness of the hollow fiber oxygen permeable membrane 301 is 0.16 mm.

[0083] The method for producing oxygen using an in-situ carbon dioxide ionization oxygen generator comprises the following steps:

[0084] S1. The CO2-containing gas in the gas inlet tank 1 is adjusted to a pressure of 300 Pa and delivered to the plasma discharge chamber 2 at a stable flow rate of 150 sccm to simulate the Martian gas environment. The current of the electrode 202 is set to 0.22 A. Ionization is performed in the 2L plasma discharge chamber 2 at 200°C. The reaction takes 2 minutes to reach equilibrium, thereby obtaining ionized gas containing oxygen.

[0085] S2. The ionized gas containing oxygen is transported to the oxygen permeable membrane reactor 3. The heating jacket 4 is then turned on. Under heating conditions of 750° C., the ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane 301. The oxygen enters the hollow fiber oxygen permeable membrane 301, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane 301. The vacuum pump 6 is turned on to absorb the oxygen. The oxygen is collected by the cluster column 302 and separated from the gas outlet 3042 through the transmission pipe 3043.

[0086] S3, the oxygen sucked by the vacuum pump 6 continuously enters the gas collecting bottle 5, and the remaining gas in the oxygen permeable membrane reactor 3 is recovered into the tail gas bottle 7 through the tail gas hole 3041.

[0087] The hollow fiber oxygen permeable membrane 301 was tested by SEM and TEM. The test results are as follows: Figure 10-13 、 Figure 18 shown.

[0088] Example 2

[0089] The method for producing oxygen using the carbon dioxide in-situ ionization oxygen generator described in Example 1 comprises the following steps:

[0090] S1. The CO2-containing gas in the gas inlet tank 1 is adjusted to a pressure of 350 Pa and a flow rate of 200 sccm is stabilized and delivered to the plasma discharge chamber 2 to simulate the Martian gas environment. The current of the electrode 202 is set to 0.25 A. Ionization is performed in the 2L plasma discharge chamber 2 at 220°C. The reaction takes 3 minutes to reach equilibrium, thereby obtaining ionized gas containing oxygen.

[0091] S2. The ionized gas enters the oxygen permeable membrane reactor 3 through the air inlet 3031. The heating jacket 4 is then turned on and heated at 800°C. The ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane 301. The oxygen enters the hollow fiber oxygen permeable membrane 301, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane 301. The vacuum pump 6 is turned on to absorb the oxygen. The oxygen is collected by the cluster column 302 and separated from the air outlet 3042 through the transmission pipe 3043.

[0092] S3, the oxygen sucked by the vacuum pump 6 continuously enters the gas collecting bottle 5, and the remaining gas in the oxygen permeable membrane reactor 3 is recovered into the tail gas bottle 7 through the tail gas hole 3041.

[0093] Example 3

[0094] The method for producing oxygen using the carbon dioxide in-situ ionization oxygen generator described in Example 1 comprises the following steps:

[0095] S1. The CO2-containing gas in the gas inlet tank 1 is adjusted to a pressure of 300 Pa and delivered to the plasma discharge chamber 2 at a stable flow rate of 150 sccm to simulate the Martian gas environment. The current of the electrode 202 is set to 0.22 A. Ionization is performed in the 2L plasma discharge chamber 2 at 210°C. The reaction takes 3 minutes to reach equilibrium, thereby obtaining ionized gas containing oxygen.

[0096] S2. The ionized gas enters the oxygen permeable membrane reactor 3 through the air inlet 3031. The heating jacket 4 is then turned on and heated at 850°C. The ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane 301. The oxygen enters the hollow fiber oxygen permeable membrane 301, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane 301. The vacuum pump 6 is turned on to absorb the oxygen. The oxygen is collected by the cluster column 302 and separated from the air outlet 3042 through the transmission pipe 3043.

[0097] S3, the oxygen sucked by the vacuum pump 6 continuously enters the gas collecting bottle 5, and the remaining gas in the oxygen permeable membrane reactor 3 is recovered into the tail gas bottle 7 through the tail gas hole 3041.

[0098] Example 4

[0099] The method for producing oxygen using the carbon dioxide in-situ ionization oxygen generator described in Example 1 comprises the following steps:

[0100] S1. The CO2-containing gas in the gas inlet tank 1 is adjusted to a pressure of 250 Pa and a flow rate of 50 sccm to be delivered to the plasma discharge chamber 2 to simulate the Martian gas environment. The current of the electrode 202 is set to 0.2 A. Ionization is performed in the 2L plasma discharge chamber 2 at 180°C. The reaction takes 5 minutes to reach equilibrium, thereby obtaining ionized gas containing oxygen.

[0101] S2. The ionized gas enters the oxygen permeable membrane reactor 3 through the air inlet 3031. The heating jacket 4 is then turned on and heated at 900°C. The ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane 301. The oxygen enters the hollow fiber oxygen permeable membrane 301, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane 301. The vacuum pump 6 is turned on to absorb the oxygen. The oxygen is collected by the cluster column 302 and separated from the air outlet 3042 through the transmission pipe 3043.

[0102] S3, the oxygen sucked by the vacuum pump 6 continuously enters the gas collecting bottle 5, and the remaining gas in the oxygen permeable membrane reactor 3 is recovered into the tail gas bottle 7 through the tail gas hole 3041.

[0103] Example 5

[0104] The method for producing oxygen using the carbon dioxide in-situ ionization oxygen generator described in Example 1 comprises the following steps:

[0105] S1. The CO2-containing gas in the gas inlet tank 1 is adjusted to a pressure of 300 Pa and delivered to the plasma discharge chamber 2 at a stable flow rate of 150 sccm to simulate the Martian gas environment. The current of the electrode 202 is set to 0.25 A. Ionization is performed in the 2L plasma discharge chamber 2 at 200°C. The reaction takes 2 minutes to reach equilibrium, thereby obtaining ionized gas containing oxygen.

[0106] S2. The ionized gas enters the oxygen permeable membrane reactor 3 through the air inlet 3031. The heating jacket 4 is then turned on and heated at 950°C. The ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane 301. The oxygen enters the hollow fiber oxygen permeable membrane 301, and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane 301. The vacuum pump 6 is turned on to absorb the oxygen. The oxygen is collected by the cluster column 302 and separated from the air outlet 3042 through the transmission pipe 3043.

[0107] S3, the oxygen sucked by the vacuum pump 6 continuously enters the gas collecting bottle 5, and the remaining gas in the oxygen permeable membrane reactor 3 is recovered into the tail gas bottle 7 through the tail gas hole 3041.

[0108] The gas in the gas collecting bottle 5 in Examples 1-5 was tested for concentration respectively. Nitrogen was used as the purge gas to test the gas composition and concentration in the gas collecting bottle 5 to obtain the content data of the relevant gas, as shown in Table 1 and Figure 14-17 、 Figure 19 shown.

[0109]

[0110] Example 6

[0111] La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material preparation process includes the following steps:

[0112] In step a2, 120 g of ethylene glycol dispersant and 100 g of citric acid complexing agent were added; in step a4, oxide D was calcined at 1000° C. for 4.5 h, and the remaining operations were the same as in Example 1; La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder particle size is 60nm;

[0113] The preparation steps of the hollow fiber oxygen permeable membrane 301 are as follows:

[0114] La in step b1 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder and ZnO were mixed in a mass ratio of 7.5:2.5 to obtain 80 g of mixed powder E; in step b2, 10 g of polyethersulfone and 40 g of N-methylpyrrolidone were mixed; in step b4, the casting solution G was degassed under vacuum for 1 h, and then nitrogen gas with a pressure of 0.2 MPa was introduced; in step b5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The mass ratio of the powder to 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol, and polyvinyl butyral is 1:1.2:1:0.6:0.9:1:1.2; the drying temperature in step b6 is 70°C; the sintering temperature in step b7 is 1100°C, and the sintering time is 5.5 hours; the remaining operations are the same as in Example 1, and a hollow fiber oxygen permeable membrane 301 with an outer diameter of a through hole of 1.60 mm and a thickness of 0.16 mm is obtained.

[0115] Example 7

[0116] La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material preparation process includes the following steps:

[0117] In step a2, 100 g of ethylene glycol dispersant and 100 g of citric acid complexing agent were added; in step a4, oxide D was calcined at 900° C. for 5 h, and the remaining operations were the same as in Example 1; La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder particle size is 40nm;

[0118] The preparation steps of the hollow fiber oxygen permeable membrane 301 are as follows:

[0119] La in step b1 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder and ZnO were mixed in a mass ratio of 8:2 to obtain 80 g of mixed powder E; in step b2, 10 g of polyethersulfone and 45 g of N-methylpyrrolidone were mixed; in step b4, the casting solution G was degassed under vacuum for 2 h, and then nitrogen gas with a pressure of 0 MPa was introduced; in step b5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The mass ratio of the powder to 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol, and polyvinyl butyral is 1:1:1.5:0.8:0.6:0.5:1.5; the drying temperature in step b6 is 90°C; the sintering temperature in step b7 is 1100°C, and the sintering time is 4.5 hours. The remaining operations are the same as in Example 1; a hollow fiber oxygen permeable membrane 301 having a through-hole outer diameter of 1.55 mm and a thickness of 0.15 mm is obtained.

[0120] Example 8

[0121] La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material preparation process includes the following steps:

[0122] In step a2, 110 g of ethylene glycol dispersant and 100 g of citric acid complexing agent were added; in step a4, oxide D was calcined at 900° C. for 5 h, and the remaining operations were the same as in Example 1; La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder particle size is 30nm;

[0123] The preparation steps of the hollow fiber oxygen permeable membrane 301 are as follows:

[0124] La in step b1 0.3 Ca0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder and ZnO were mixed in a mass ratio of 7:3 to obtain 80 g of mixed powder E; in step b2, 10 g of polyethersulfone and 50 g of N-methylpyrrolidone were mixed; in step b4, the casting solution G was degassed under vacuum for 2 h, and then nitrogen gas with a pressure of 0 MPa was introduced; in step b5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The mass ratio of the powder to 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol, and polyvinyl butyral was 1:0.8:1.3:0.5:0.9:0.7:1.3; the drying temperature in step b6 was 75°C; the sintering temperature in step b7 was 1150°C, and the sintering time was 5 hours. The remaining operations were the same as in Example 1; and a hollow fiber oxygen permeable membrane 301 having an outer diameter of a through hole of 1.6 mm and a thickness of 0.155 mm was obtained.

[0125] Comparative Example 1

[0126] No bismuth nitrate was added in step a1, and the remaining operations were the same as in Example 6 to obtain a permeable membrane.

[0127] Comparative Example 2

[0128] Neodymium nitrate was not added in step a1, and the remaining operations were the same as in Example 6 to obtain a permeable membrane.

[0129] Comparative Example 3

[0130] In step a1, neodymium nitrate and bismuth nitrate are not added, and the remaining operations are the same as those in Example 6 to obtain a permeable membrane.

[0131] Comparative Example 4

[0132] Calcium nitrate was not added in step a1, and the remaining operations were the same as in Example 6 to obtain a permeable membrane.

[0133] The hollow fiber oxygen permeable membranes 301 prepared in Examples 6-8 and the permeable membranes prepared in Comparative Examples 1-4 were respectively subjected to the method of Example 3 for the production of O2 from CO2, with nitrogen used as the purge gas. The collected gas was tested, and the data obtained are shown in Table 2.

[0134]

[0135] As can be seen from the above, the hollow fiber oxygen permeable membrane 301 provided in the present invention can effectively separate oxygen, and the obtained oxygen content is high, and can realize the preparation and separation of oxygen at different temperatures and different carbon dioxide concentrations, thereby realizing the preparation and separation and purification of oxygen in the Martian environment. In addition, the present invention adopts a stable material to prepare the oxygen permeable membrane reactor 3, which can ensure the oxygen permeability while being able to operate stably in an acidic atmosphere for a long time. Figure 19 It can be seen that the stable operation time is more than 3000 hours.

Claims

1. A carbon dioxide in-situ ionization oxygen production device, comprising an air inlet tank (1) and a plasma discharge chamber (2), characterized in that: The gas inlet tank (1) is connected to the plasma discharge chamber (2), the plasma discharge chamber (2) is connected to an oxygen permeable membrane reactor (3), a heating jacket (4) is provided on the outside of the oxygen permeable membrane reactor (3), the oxygen permeable membrane reactor (3) is connected to a gas collecting bottle (5), and a vacuum pump (6) is connected between the oxygen permeable membrane reactor (3) and the gas collecting bottle (5); an electrode (202) is provided inside the plasma discharge chamber (2), the electrode (202) is connected to a plasma power supply (201), and a plurality of hollow fiber oxygen permeable membranes (301) are provided inside the oxygen permeable membrane reactor (3). If The dry hollow fiber oxygen permeable membrane (301) is fixed on the cluster column (302), and the left and right ends of the oxygen permeable membrane reactor (3) are respectively fixed with a vacuum sealing head 1 (303) and a vacuum sealing head 2 (304), the vacuum sealing head 1 (303) is connected to the plasma discharge chamber (2), the vacuum sealing head 2 (304) is connected to the vacuum pump (6), and the cluster column (302) is connected to the vacuum sealing head 2 (304); the hollow fiber oxygen permeable membrane (301) is supported by a zinc oxide composite material, and a through hole is opened on the support body. The composite material is composed of ZnO-La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ A separation functional layer is set on the outer surface of the support body. The material of the separation functional layer is La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ .

2. The carbon dioxide in-situ ionization oxygen production device according to claim 1, characterized in that: An air inlet (3031) is provided on the top of the first vacuum sealing head (303), an exhaust hole (3041) is provided on the top of the second vacuum sealing head (304), an air outlet (3042) is provided on the side of the second vacuum sealing head (304), and a transmission tube (3043) is provided inside the second vacuum sealing head (304), one end of the transmission tube (3043) is connected to the cluster column (302), and the other end passes through the air outlet (3042) to be connected to the vacuum pump (6).

3. The carbon dioxide in-situ ionization oxygen production device according to claim 2, characterized in that: The tail gas hole (3041) is connected to the tail gas bottle (7).

4. The carbon dioxide in-situ ionization oxygen production device according to claim 1, characterized in that: A gas flow meter 1 (101) is connected between the gas inlet tank (1) and the plasma discharge chamber (2), and a gas flow meter 2 (203) is connected between the plasma discharge chamber (2) and the oxygen permeable membrane reactor (3).

5. The carbon dioxide in-situ ionization oxygen production device according to claim 1, characterized in that: The inner wall of the vacuum sealing head 1 (303), the inner wall of the vacuum sealing head 2 (304) and the outer wall of the oxygen permeable membrane reactor (3) are made of quartz; La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The material preparation process includes the following steps: a1. Adding a mixture of lanthanum nitrate, calcium nitrate, strontium nitrate, bismuth nitrate, neodymium nitrate, cobalt nitrate and ferric nitrate to deionized water to form a uniform mixed solution B; a2. Add ethylene glycol dispersant and citric acid complexing agent to the mixed solution B obtained in step a1, adjust to neutrality with aqueous ammonia, and continue heating and stirring until a gel solution C is formed; a3. Heat and dry the gel solution C obtained in step a2 until powdered oxide D is formed; a4. After calcining the powdered oxide D obtained in step a3, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ Powder, particle size 20-60nm.

6. The carbon dioxide in-situ ionization oxygen production device according to claim 5, characterized in that: The mass ratio of the metal salt in step a1 to the ethylene glycol dispersant and the citric acid complexing agent in step a2 is 1:1-1.5:1; the powder oxide D in step a4 is calcined at a temperature of 800-1000°C for a time of 4.5-5 hours. The preparation steps of the hollow fiber oxygen permeable membrane (301) are as follows: b1. La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder and ZnO are mixed to obtain mixed powder E; b2. Mix polyethersulfone and N-methylpyrrolidone and stir until they are completely dissolved to form a transparent solution F; b3. Add the mixed powder E to the solution F in batches and continue stirring to form a casting solution G; b4. Degas the casting solution G under vacuum, then introduce nitrogen, use N-methylpyrrolidone and ethanol as the core solution and inner coagulation bath, and water as the outer coagulation bath. Driven by pressure, the casting solution is uniformly extruded through a spinneret into the outer coagulation bath, soaked and dried, to obtain the support precursor H; b5, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The powder is mixed evenly with 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol and polyvinyl butyral to obtain an impregnation solution I; b6. Immersing the support precursor H in the impregnation solution I, then pulling it out, and repeating the above pulling process after drying to obtain the hollow fiber precursor J; b7. Sintering the hollow fiber precursor J to obtain a hollow fiber oxygen permeable membrane (301).

7. The carbon dioxide in-situ ionization oxygen production device according to claim 6, characterized in that: The outer diameter of the through hole of the hollow fiber oxygen permeable membrane (301) is 1.50-1.60 mm, and the thickness of the hollow fiber oxygen permeable membrane (301) is 0.15-0.16 mm; in step b1, La 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The mass ratio of powder to ZnO is 7-8:2-3; the mass ratio of polyethersulfone, N-methylpyrrolidone and mixed powder E in step b1 in step b2 is 1:4-5:8; the vacuum degassing time in step b4 is 1-2h, and the nitrogen pressure is 0-0.2MPa; La in step b5 0.3 Ca 0.1 Sr 0.2 Bi 0.2 Nd 0.2 Co 0.3 Fe 0.7 O 3-δ The mass ratio of the powder to 2-butanone, ethanol, triethanolamine, dibutyl phthalate, polyethylene glycol and polyvinyl butyral is 1:0.8-1.2:1-1.5:0.5-0.8:0.6-0.9:0.5-1:1.2-1.5; the drying temperature in step b6 is 70-90°C; the sintering temperature in step b7 is 1100-1200°C, and the sintering time is 4.5-5.5h.

8. A method for producing oxygen using the carbon dioxide in-situ ionization oxygen production device according to any one of claims 1 to 7, characterized in that: The following steps are involved: S1, pressurizing and transporting the CO2-containing gas in the gas inlet tank (1) into the plasma discharge chamber (2), and performing an ionization reaction to obtain an ionized gas containing oxygen; S2, transporting the ionized gas containing oxygen to the oxygen permeable membrane reactor (3), wherein under heating conditions, the ionized gas containing oxygen selectively permeates the surface of the hollow fiber oxygen permeable membrane (301), and the oxygen enters the interior of the hollow fiber oxygen permeable membrane (301), and the remaining gas accumulates outside the hollow fiber oxygen permeable membrane (301); S3. Collect oxygen into the gas collecting bottle (5), and recover the remaining gas into the tail gas bottle (7).

9. The method for producing oxygen using the carbon dioxide in-situ ionization oxygen generator according to claim 8, characterized in that: In step S1, the pressure of the CO2-containing gas is 250-350 Pa, the ionization reaction temperature is 180-220° C., the reaction time is 2-5 min, the reaction current is 0.2-0.25 A, and the flow rate of the CO2-containing gas is 50-200 sccm.

10. The method for producing oxygen using the carbon dioxide in-situ ionization oxygen production device according to claim 8, characterized in that: The heating temperature in step S2 is 750-950°C.

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