A specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption.

Abstract

This invention relates to the field of molecular sieve technology and discloses a specialized molecular sieve for separating ozone and oxygen via pressure swing adsorption (PSA). The molecular sieve is resistant to the strong oxidizing properties of ozone, exhibits strong ozone adsorption under certain pressure, and does not adsorb oxygen. The molecular sieve comprises silica, alumina, composite metal oxides, and silicates, wherein the composite metal oxides are composed of transition metal oxides and rare earth metal oxides. The specialized molecular sieve prepared by this invention can significantly improve ozone separation efficiency. Through unique component formulation and by controlling the proportions of silica, alumina, composite metal oxides, and silicates, combined with a special crystal structure, it exhibits extremely strong ozone adsorption under certain pressure while almost completely excluding oxygen. This means that in practical applications, high concentrations of ozone can be obtained with lower energy consumption and cost, greatly improving the efficiency of ozone utilization in various industries.

Description

Technical Field

[0001] This invention relates to the field of molecular sieve technology, specifically a specialized molecular sieve for separating ozone and oxygen via pressure swing adsorption (PSA). Background Technology

[0002] In modern industrial production systems, ozone has extremely wide applications, ranging from wastewater treatment and food processing disinfection to fine chemical synthesis, all relying on its strong oxidizing properties to achieve specific production goals. Industrial ozone generators using oxygen sources are one of the main sources of ozone, producing a mixture of ozone and oxygen, with an ozone concentration typically around 148 mg / L, approximately 10% ozone and 90% oxygen. This low concentration of ozone presents several limitations in practical applications. In wastewater treatment, achieving ideal disinfection and pollutant degradation requires a larger amount of ozone, increasing energy consumption and extending treatment time. In food processing disinfection, low-concentration ozone may not completely kill harmful microorganisms, affecting food safety, while increasing ozone concentration leads to a significant increase in costs. Simultaneously, the direct emission of large amounts of underutilized oxygen not only wastes resources but also increases production costs.

[0003] Molecular sieves, as key materials in gas separation, have been extensively researched and applied over the past few decades. Traditional molecular sieves are mainly used for drying and purifying gases, as well as in catalytic cracking processes in petrochemicals. However, traditional molecular sieves have significant limitations in separating ozone and oxygen mixtures. The pore size distribution and surface properties of ordinary molecular sieves make it difficult to selectively adsorb ozone, thus hindering efficient separation. Some molecular sieves with certain adsorption properties exhibit poor structural stability under the strong oxidizing environment of ozone, easily undergoing degradation and deactivation, resulting in short service life and high costs.

[0004] Existing gas separation technologies also face numerous challenges when processing mixtures of ozone and oxygen. For example, cryogenic distillation, while theoretically capable of separating the two, requires extremely low temperatures and high pressures, resulting in large, complex equipment, high energy consumption, and stringent process requirements. The investment and operating costs are prohibitive for many companies. Membrane separation technology, while relatively simple to operate, has limited separation efficiency and cannot meet the demands of large-scale industrial production for high-purity ozone and oxygen.

[0005] Therefore, it is of great significance to develop a technology that can efficiently separate ozone and oxygen, increase ozone concentration, and realize oxygen recovery and utilization. Summary of the Invention

[0006] To address the problems in the prior art, this invention provides a specialized molecular sieve for separating ozone and oxygen via pressure swing adsorption (PSA).

[0007] The technical solution adopted by the present invention to solve its technical problem is: a special molecular sieve for separating ozone and oxygen by pressure swing adsorption (PSA). The molecular sieve is resistant to the strong oxidizing properties of ozone, has strong adsorption properties for ozone under certain pressure and does not adsorb oxygen.

[0008] The molecular sieve components, by weight percentage, include 30-45% silicon dioxide, 15-25% alumina, and 5-15% composite metal oxides, with the balance being silicates. The composite metal oxides are composed of transition metal oxides and rare earth metal oxides.

[0009] Silica, alumina, composite metal oxides, and silicates work synergistically to form a stable structure with unique adsorption properties. The transition metal oxides and rare earth metal oxides in the composite metal oxides introduce special active sites into the crystal structure, enhancing the molecular sieve's adsorption capacity for ozone while preventing the adsorption of oxygen. This characteristic allows the molecular sieve to selectively adsorb ozone in the separation of ozone and oxygen mixtures, achieving highly efficient separation of the two gases.

[0010] As a further technical solution, the transition metal oxide is copper oxide and zinc oxide;

[0011] The mass ratio of copper oxide to zinc oxide is 3-4:1. Copper oxide and zinc oxide can form specific microstructures in the molecular sieve structure, enhancing the adsorption affinity for ozone molecules. Simultaneously, the appropriate ratio ensures the synergistic effect between the two oxides, making the molecular sieve more stable in adsorbing ozone, significantly improving the adsorption capacity and rate of ozone, and thus enhancing the overall separation efficiency.

[0012] As a further technical solution, the rare earth metal oxide is cerium oxide and lanthanum oxide;

[0013] The mass ratio of cerium oxide to lanthanum oxide is 2:1-1.2. Cerium oxide and lanthanum oxide are selected as the rare earth metal oxides. In the molecular sieve, cerium oxide and lanthanum oxide can adjust the surface acidity / alkalinity and electronic properties of the crystals, further optimizing the ozone adsorption performance of the molecular sieve. At this ratio, cerium oxide and lanthanum oxide work synergistically to effectively enhance the redox capacity of the molecular sieve, making it easier for ozone to interact with the molecular sieve surface during adsorption, thereby improving the selectivity and stability of ozone adsorption. This optimized ratio helps to achieve more stable separation of ozone and oxygen in complex industrial environments, reducing the impact of impurity gases on the separation effect.

[0014] As a further technical solution, the method for preparing the special molecular sieve includes the following steps:

[0015] Silicate ore is pulverized to 200-300 mesh. Silicate, silicon dioxide, alumina powder, and a nitrate compound containing composite metal elements are weighed out, and the nitrate compound is prepared into a metal ion solution. Each step of this preparation method works in close coordination to create the excellent properties of the molecular sieve. Pulverizing the silicate ore increases the specific surface area of ​​the raw materials, allowing them to participate more fully in subsequent reactions and ensuring uniform mixing of all components. Preparing the nitrate compound into a metal ion solution facilitates the uniform distribution of the composite metal elements within the molecular sieve, ensuring effective control over its adsorption performance.

[0016] The powder and metal ion solution were mixed evenly, and then a binder and a pore-forming agent were added. After stirring, the mixture was extruded and molded to obtain a molecular sieve precursor.

[0017] Adding binders and pore-forming agents enhances the bonding force between components and ensures the structural stability of the molecular sieve; the pore-forming agent decomposes during calcination to form a uniform microporous structure, increasing the specific surface area and improving the adsorption capacity.

[0018] The molecular sieve precursor was dried at 112-120℃ for 8-10 hours, and then heated to 550-700℃ at a heating rate of 2-3℃ / min for 3-4 hours. The drying and calcination processes further optimized the crystal structure of the molecular sieve, making it more stable and enhancing its ozone adsorption performance.

[0019] The calcined molecular sieve is cooled to room temperature and then completely soaked in a 5-5.8% silane coupling agent solution at a material-to-liquid ratio of 1:10-12 for 1-1.5 hours. It is then dried at 80-90℃ for 3-4 hours to obtain the final silane coupling agent treatment. This treatment improves the surface properties of the molecular sieve, enhances its water resistance and chemical stability, and extends its service life.

[0020] As a further technical solution, the binder is boehmite, and the amount of binder is 4-4.6% of the total mass of the raw materials. Boehmite is chosen as the binder because it undergoes a phase transition during heating to generate alumina, which not only enhances the bonding force between the raw materials but also forms chemical bonds with other components in the molecular sieve, further stabilizing the structure of the molecular sieve. Within this dosage range, it ensures that the components are tightly bound without clogging the pores of the molecular sieve due to excessive binder, thus affecting its adsorption performance. This precise dosage control helps to prepare molecular sieves with stable structure and good adsorption performance, improving product quality and stability.

[0021] As a further technical solution, the pore-forming agent is polyethylene glycol (PEG), and the amount of pore-forming agent used is 3-4% of the total mass of the raw materials. PEG plays a crucial role as a pore-forming agent in the preparation process. During calcination, PEG decomposes and volatilizes, leaving uniformly distributed pores. The size and number of these pores directly affect the specific surface area and adsorption performance of the molecular sieve. This dosage range can form micropores of suitable size and quantity, which is beneficial for the diffusion and adsorption of ozone molecules, while ensuring the mechanical strength of the molecular sieve. If the amount of pore-forming agent is too much or too little, it will lead to an undesirable pore structure, thereby reducing the adsorption efficiency and separation effect of the molecular sieve.

[0022] As a further technical solution, during the extrusion molding process, the screw speed is 20-25 r / min and the extrusion pressure is 2-3 MPa. Under these parameters, the mixed raw materials can be evenly distributed in the mold, forming a molecular sieve precursor with uniform texture. Appropriate screw speed and extrusion pressure ensure the density and shape stability of the precursor, avoiding internal defects or uneven structures. This uniform structure facilitates uniform heat transfer and material migration during subsequent drying and calcination processes, further promoting the formation and improvement of the molecular sieve crystal structure, ultimately enhancing the adsorption performance and mechanical strength of the molecular sieve, ensuring stable and efficient operation in practical applications.

[0023] As a further technical solution, a method for separating ozone and oxygen using a dedicated molecular sieve includes the following steps: passing a mixture of ozone and oxygen into a separation device consisting of 2-8 adsorption towers and a buffer tank;

[0024] Inside the adsorption tower, ozone is adsorbed by the molecular sieve, while oxygen flows out into the buffer tank. When the molecular sieve in the adsorption tower reaches adsorption saturation, the pressure inside the adsorption tower is reduced to 0.1-0.2 MPa to desorb the ozone, which is then collected and utilized.

[0025] Control the switching between adsorption and desorption in the adsorption tower, with an adsorption time of 20-30 minutes and a desorption time of 5-8 minutes.

[0026] As a further technical solution, the flow rate of the ozone and oxygen mixture entering the adsorption tower is 0.3-0.5 m³ / s. 3 The flow rate range of / h is determined by comprehensively considering factors such as the adsorption capacity of the molecular sieve, the processing capacity of the adsorption tower, and the separation efficiency. If the flow rate is too low, production efficiency will be reduced; if the flow rate is too high, the contact time between the mixed gas and the molecular sieve will be too short, and the ozone will flow out of the adsorption tower before it is fully adsorbed, reducing the separation effect. Within this flow rate range, the mixed gas can fully contact the molecular sieve, enabling the molecular sieve to effectively adsorb ozone, while ensuring the stability and efficiency of the entire separation process, which is conducive to realizing large-scale industrial production.

[0027] The beneficial effects of this invention are:

[0028] The specialized molecular sieve prepared by this invention can significantly improve ozone separation efficiency. Through unique component formulation, by controlling the proportions of silica, alumina, composite metal oxides, and silicates, and with a special crystal structure, it exhibits extremely strong ozone adsorption capacity under certain pressure, while almost not adsorbing oxygen. This means that in practical applications, high concentrations of ozone can be obtained with lower energy consumption and cost, greatly improving the efficiency of ozone utilization in various industries.

[0029] Each step in the molecular sieve preparation process plays a crucial role in ensuring its performance. Crushing the silicate ore increases the specific surface area of ​​the raw materials, allowing for more complete participation in subsequent reactions and promoting uniform mixing of components. Precise weighing of various raw materials and preparation of nitrate compounds into metal ion solutions ensures the uniform distribution of composite metal oxides within the molecular sieve, enhancing its ozone adsorption selectivity and stability. The addition of boehmite as a binder and polyethylene glycol as a pore-forming agent enhances the binding force between components during the mixing and molding process, ensuring structural stability of the molecular sieve during use. Polyethylene glycol decomposes and volatilizes during calcination, forming a uniform microporous structure, increasing the specific surface area of ​​the molecular sieve, and improving its adsorption capacity. The drying and calcination steps further optimize the crystal structure of the molecular sieve, enabling it to remain stable even under the strong oxidizing environment of ozone and extending its service life.

[0030] This invention not only achieves efficient ozone separation but also enables the recovery and reuse of the separated oxygen. Through pressure swing adsorption (PSA), high-purity oxygen is collected simultaneously with ozone separation, preventing oxygen waste. The separated oxygen is of high purity, and this recovered oxygen can be reused in other stages of industrial production, such as as a combustion aid, reducing the company's dependence on external oxygen supplies, further saving production costs, and achieving efficient resource utilization. Detailed Implementation

[0031] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. 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.

[0032] This invention provides a specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption, along with its preparation and separation methods. The details are as follows:

[0033] Composition and characteristics of the specialized molecular sieve: The specialized molecular sieve of this invention is resistant to the strong oxidizing properties of ozone, exhibits strong ozone adsorption under certain pressure, and does not adsorb oxygen. Its composition, by weight percentage, includes 30-45% silicon dioxide, 15-25% alumina, 5-15% composite metal oxides, and the balance being silicates. The composite metal oxides consist of transition metal oxides and rare earth metal oxides; the transition metal oxides are copper oxide and zinc oxide, with a mass ratio of 3-4:1; the rare earth metal oxides are cerium oxide and lanthanum oxide, with a mass ratio of 2:1-1.2.

[0034] Preparation method of special molecular sieve

[0035] Raw material pretreatment: Select suitable silicate ore and crush it to 200-300 mesh. Accurately weigh silicate, silicon dioxide, alumina powder, and nitrate compound containing complex metal elements according to the formula ratio. Dissolve the nitrate compound in an appropriate amount of deionized water to prepare a metal ion solution.

[0036] Mixing and Molding: Weigh the silicate, silica, and alumina powders and add them to a mixing device, stirring until homogeneous. Then, slowly add the prepared metal ion solution, stirring continuously to ensure thorough mixing of the solution and powders. Next, add the binder (boehmite) and the pore-forming agent (polyethylene glycol). The binder dosage is 4-4.6% of the total raw material mass, and the pore-forming agent dosage is 3-4% of the total raw material mass. Continue stirring for a period of time to ensure uniform mixing of all components. Place the resulting mixture into an extrusion molding device, setting the screw speed to 20-25 r / min and the extrusion pressure to 2-3 MPa, and extrude to obtain the molecular sieve precursor.

[0037] Drying and calcination: The molecular sieve precursor is placed in an oven and dried at 112-120℃ for 8-10 hours to remove moisture. The dried precursor is then transferred to a muffle furnace and heated to 550-700℃ at a heating rate of 2-3℃ / min for calcination for 3-4 hours to induce physical and chemical changes in the precursor and form a stable molecular sieve structure.

[0038] Post-processing: After calcination, the molecular sieve is naturally cooled to room temperature, and then immersed in a 5-5.8% (w / w) silane coupling agent solution at a material-to-liquid ratio of 1:10-12 for 1-1.5 hours. After immersion, it is removed and dried in an oven at 80-90℃ for 3-4 hours to obtain the final special molecular sieve product.

[0039] A method for separating ozone and oxygen using specialized molecular sieves: Construct a separation device consisting of 2-8 adsorption towers and a buffer tank. The ozone and oxygen mixture is then dispersed at a flow rate of 0.3-0.5 m³ / s. 3A flow rate of [amount] / h is fed into the adsorption tower of the separation unit. Inside the adsorption tower, due to the characteristics of the specialized molecular sieve, ozone is adsorbed by the sieve, while oxygen flows out and enters the buffer tank. When the molecular sieve in the adsorption tower reaches adsorption saturation, the pressure inside the adsorption tower is reduced to 0.1-0.2 MPa, causing the adsorbed ozone to desorb. The high-concentration ozone gas desorbed is collected and utilized. A control device precisely controls the switching between adsorption and desorption in the adsorption tower, setting the adsorption time to 20-30 minutes and the desorption time to 5-8 minutes, achieving continuous and efficient separation of ozone and oxygen.

[0040] To further illustrate the present invention, the following embodiments provide a detailed description. The silicate ore, silicon dioxide, alumina powder, nitrate compounds containing composite metal elements, boehmite, polyethylene glycol, silane coupling agents, and other raw materials used in the following embodiments of the present invention are all commercially available conventional products.

[0041] The following are specific examples:

[0042] Example 1

[0043] Preparation of special molecular sieves

[0044] Raw material preparation: Crush the silicate ore to 200 mesh, and weigh out 32% silicate, 42% silicon dioxide, and 20% alumina powder. Weigh out an appropriate amount of nitrate compound containing copper, zinc, cerium, and lanthanum elements, and prepare a metal ion solution, wherein the mass ratio of copper oxide to zinc oxide is 3.2:1, and the mass ratio of cerium oxide to lanthanum oxide is 2:1.1.

[0045] Mixing and molding: After the powder is mixed evenly, a metal ion solution is added and stirred evenly. 4.3% boehmite and 3.2% polyethylene glycol (by mass of the total raw materials) are added, and the mixture is extruded at a screw speed of 22 r / min and an extrusion pressure of 2.3 MPa.

[0046] Drying and calcination: Dry at 116℃ for 8.5 hours, then calcin at 620℃ for 3.2 hours with the temperature increased at 2.2℃ / min.

[0047] Post-treatment: After cooling, soak in a 5.2% silane coupling agent solution at a material-to-liquid ratio of 1:10.5 for 1.3 hours, and then dry at 86℃ for 3.3 hours.

[0048] Ozone and oxygen separation: A separation device consisting of 5 adsorption towers and a buffer tank is used, with a mixed gas flow rate of 0.4 m³ / s. 3 / h, adsorption time 23 minutes, desorption pressure 0.13 MPa, desorption time 6.5 minutes.

[0049] Example 2

[0050] Preparation of special molecular sieves

[0051] Raw material preparation: Crush silicate ore to 250 mesh, and weigh out 35% silicate, 40% silicon dioxide, and 18% alumina powder. Prepare a metal ion solution with a copper oxide to zinc oxide mass ratio of 3.5:1 and a cerium oxide to lanthanum oxide mass ratio of 2:1.

[0052] Mixing and molding: Mix the powder and solution, add 4.5% boehmite and 3.5% polyethylene glycol, screw speed 23 r / min, extrusion pressure 2.5 MPa for molding.

[0053] Drying and calcination: Dry at 118℃ for 9 hours, then heat to 650℃ at a rate of 2.5℃ / min and calcin for 3.5 hours.

[0054] Post-treatment: Soak in 5.5% silane coupling agent solution at a material-to-liquid ratio of 1:11 for 1.2 hours, and dry at 88℃ for 3.5 hours.

[0055] Separating ozone and oxygen: using 6 adsorption towers, with a mixed gas flow rate of 0.45 m³ / h. 3 / h, adsorption time 26 minutes, desorption pressure 0.15MPa, desorption time 7 minutes.

[0056] Example 3

[0057] Preparation of special molecular sieves

[0058] Raw material preparation: Crush the ore to 280 mesh, and weigh out 38% silicate, 38% silicon dioxide, and 16% alumina powder. The mass ratio of copper oxide to zinc oxide in the metal ion solution is 3.8:1, and the mass ratio of cerium oxide to lanthanum oxide is 2:1.2.

[0059] Mixing and molding: Add 4.1% boehmite and 3.8% polyethylene glycol, screw speed 21 r / min, extrusion pressure 2.2 MPa for molding.

[0060] Drying and calcination: Dry at 114℃ for 9.5 hours, then heat to 580℃ at a rate of 2.3℃ / min and calcin for 3.8 hours.

[0061] Post-treatment: Soak in 5.3% silane coupling agent solution at a material-to-liquid ratio of 1:11.5 for 1.4 hours, and dry at 82℃ for 3.7 hours.

[0062] Separating ozone and oxygen: Four adsorption towers were installed, with a mixed gas flow rate of 0.35 m³ / h. 3 / h, adsorption time 28 minutes, desorption pressure 0.12 MPa, desorption time 7.5 minutes.

[0063] Example 4

[0064] Preparation of special molecular sieves

[0065] Raw material preparation: Crush silicate ore to 300 mesh, and weigh out 40% silicate, 35% silicon dioxide, and 15% alumina powder. Prepare a metal ion solution with a copper oxide to zinc oxide mass ratio of 4:1 and a cerium oxide to lanthanum oxide mass ratio of 2:1.1.

[0066] Mixing and molding: Add 4.6% boehmite and 3% polyethylene glycol, screw speed 24 r / min, extrusion pressure 2.8 MPa for molding.

[0067] Drying and calcination: Dry at 120℃ for 8 hours, then heat to 700℃ at 3℃ / min and calcin for 3 hours.

[0068] Post-treatment: Soak in 5.8% silane coupling agent solution at a material-to-liquid ratio of 1:12 for 1 hour, and dry at 90℃ for 3 hours.

[0069] Ozone and oxygen separation: Seven adsorption towers are used, with a mixed gas flow rate of 0.5 m³ / h. 3 / h, adsorption time 20 minutes, desorption pressure 0.2 MPa, desorption time 5 minutes.

[0070] Comparative Example 1

[0071] Ozone and oxygen separation tests were conducted using a common molecular sieve (HYS-13X type molecular sieve from Shanghai Hengye Molecular Sieve Co., Ltd.), and the separation device and operating conditions were the same as in Example 2.

[0072] Comparative Example 2

[0073] In the preparation of molecular sieves, no composite metal compounds were added, and other preparation conditions and separation operations were the same as in Example 3.

[0074] test

[0075] Ozone recovery rate test

[0076] The ozone content was determined according to the relevant methods in GB / T23499-2009 "Analytical Methods for Hygienic Standards of Polyvinyl Chloride Molded Products for Food Packaging".

[0077] Experimental procedure: The ozone separated in the examples and comparative examples was collected, the ozone content was determined by chemical titration, and the ozone recovery rate was calculated.

[0078] Oxygen purity test

[0079] The method for gas purity detection is performed in accordance with GB method: GB / T3634.2-2011 "Pure hydrogen, high-purity hydrogen and ultrapure hydrogen - Part 2: Methods for purity analysis";

[0080] Experimental procedure: The purity of the separated oxygen was analyzed using a gas chromatograph;

[0081] The adsorption capacity can be determined by referring to the detection method in GB / T 7702.20-2008 "Test Methods for Determination of Adsorption Capacity of Benzene Vapor by Coal-based Granular Activated Carbon".

[0082] Table 1

[0083]

[0084] As can be seen from Table 1, the molecular sieve prepared by this invention can effectively separate ozone and oxygen.

[0085] Although embodiments of the invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption, characterized in that, The molecular sieve is resistant to the strong oxidizing properties of ozone, and under certain pressure, it has a strong adsorption capacity for ozone but does not adsorb oxygen. The molecular sieve composition, by weight percentage, includes 30-45% silicon dioxide, 15-25% aluminum oxide, and 5-15% composite metal oxide, with the balance being silicates. The composite metal oxide is composed of transition metal oxides and rare earth metal oxides; the transition metal oxides are copper oxide and zinc oxide. The mass ratio of copper oxide to zinc oxide is 3-4:1; the rare earth metal oxides are cerium oxide and lanthanum oxide. The mass ratio of cerium oxide to lanthanum oxide is 2:1-1.

2.

2. The specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption as described in claim 1, characterized in that, The method for preparing the special molecular sieve includes the following steps: The silicate ore is crushed to 200-300 mesh. Silicate, silicon dioxide, alumina powder and nitrate compound containing composite metal elements are weighed out and the nitrate compound is prepared into a metal ion solution. Silicate, silica, alumina powder, and metal ion solution are mixed evenly, then binder and pore-forming agent are added, and after stirring, the mixture is extruded to obtain molecular sieve precursor. The molecular sieve precursor is dried at 112-120℃ for 8-10 hours, and then heated to 550-700℃ at a heating rate of 2-3℃ / min for 3-4 hours. The calcined molecular sieve is cooled to room temperature, then completely soaked in a 5-5.8% silane coupling agent solution at a material-to-liquid ratio of 1:10-12 for 1-1.5 hours, and dried at 80-90℃ for 3-4 hours to obtain the final product.

3. The specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption as described in claim 2, characterized in that, The binder is boehmite, and the amount of binder used is 4-4.6% of the total mass of the raw materials.

4. The specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption as described in claim 2, characterized in that, The pore-forming agent is polyethylene glycol, and the amount of pore-forming agent used is 3-4% of the total mass of the raw materials.

5. The specialized molecular sieve for separating ozone and oxygen via PSA pressure swing adsorption as described in claim 2, characterized in that, During the extrusion molding process, the screw speed is 20-25 r / min and the extrusion pressure is 2-3 MPa.

6. A method for separating ozone and oxygen using a specialized molecular sieve according to any one of claims 1-5 via pressure swing adsorption (PSA), characterized in that, The process includes the following steps: passing a mixture of ozone and oxygen into a separation device consisting of 2-8 adsorption towers and a buffer tank; Inside the adsorption tower, ozone is adsorbed by the molecular sieve, while oxygen flows out into the buffer tank. When the molecular sieve in the adsorption tower reaches adsorption saturation, the pressure inside the adsorption tower is reduced to 0.1-0.2 MPa to desorb the ozone, which is then collected and utilized. Control the switching between adsorption and desorption in the adsorption tower, with an adsorption time of 20-30 minutes and a desorption time of 5-8 minutes.

7. The method for separating ozone and oxygen using a specialized molecular sieve via PSA pressure swing adsorption as described in claim 6, characterized in that, The flow rate of the ozone and oxygen mixture entering the adsorption tower is 0.3-0.5 m³ / s. 3 / h.

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