SSZ-13 molecular sieve membrane with high separation performance, opposite diffusion preparation method and application of SSZ-13 molecular sieve membrane in gas separation

Abstract

The invention discloses a high-separation-performance SSZ-13 molecular sieve membrane, an opposite diffusion preparation method and application of the SSZ-13 molecular sieve membrane in gas separation, and belongs to the technical field of molecular sieve membrane preparation and application. According to an opposite diffusion crystallization strategy provided by the invention, an organic template agent solution and a silicon source solution are respectively introduced into two sides of a porous alumina tube, and the SSZ-13 molecular sieve membrane is successfully synthesized, so that efficient separation of N2 in CH4 is realized. Compared with the traditional hydrothermal synthesis method, the method provided by the invention only needs 7.5 wt% of organic template agent solution, so that the use of the organic template agent can be greatly saved. In addition, the organic template agent aqueous solution which does not participate in the reaction in the porous alumina tube can be recycled, so that the utilization rate of the raw materials is further improved. According to the method provided by the invention, the use of the organic template agent is greatly reduced, and the organic template agent solution which does not participate in the reaction in the supporting tube can be recycled, so that the utilization rate of raw materials is further improved, the manufacturing cost is reduced, and the pollution is reduced.

Description

Technical Field

[0001] This invention belongs to the field of molecular sieve membrane preparation and application technology, specifically relating to a high-performance SSZ-13 molecular sieve membrane, a counter-diffusion preparation method, and its application in gas separation. This counter-diffusion preparation method can significantly reduce the use of organic template agents. Background Technology

[0002] The efficient purification of natural gas, especially for unconventional resources such as shale gas, tight gas, and coalbed methane, is a crucial step in achieving a low-carbon economic transformation. Selective removal of N2 is one of the main challenges currently facing the industry. The similar molecular size and physicochemical properties of N2 (0.36 nm) and CH4 (0.38 nm) make their separation difficult. Compared to traditional separation technologies, membrane separation is considered a promising alternative due to its advantages such as low energy consumption, small footprint, and flexible operation. Selecting high-performance membrane materials is a crucial prerequisite for achieving efficient N2 / CH4 separation.

[0003] CHA-type molecular sieve membranes, such as aluminosilicate SSZ-13 and aluminosilicate SAPO-34, exhibit the potential for efficient N2 separation from CH4 due to their regular and appropriately sized pore structure (0.38 nm × 0.38 nm). Among them, SSZ-13 zeolite with a high silica-to-alumina ratio (approximately 25–100:1) possesses excellent hydrothermal stability and hydrophobicity, making it more suitable for practical applications. Currently, SSZ-13 molecular sieve membranes are typically synthesized using a seed-assisted secondary hydrothermal method. Traditional secondary hydrothermal methods require a large amount of homogeneous synthesis solution containing expensive organic template agents to maintain solution saturation during SSZ-13 crystal growth. However, in actual synthesis, only a small amount of raw materials are converted into SSZ-13 molecular sieve membranes on the support surface; the majority of the remaining raw materials either form amorphous gels in solution or remain unreacted and difficult to recover, resulting in significant waste of organic template agents and high costs. This problem severely restricts the large-scale preparation and industrial application of SSZ-13 molecular sieve membranes. Therefore, developing an efficient synthesis method that can significantly reduce the amount of organic template agent used is of great economic and practical significance for promoting the preparation of high-performance SSZ-13 molecular sieve membranes.

[0004] Previous studies have explored synthetic routes with low template consumption. Nair et al. (Angew. Chem. Int. Ed. 2022, 61, e202204265.) proposed a "viscosity-limited dry gel conversion method" for preparing CHA-type molecular sieve membranes. This method eliminates the need for liquid-phase hydrothermal treatment, making low-cost large-scale production possible. Zhou Rongfei et al. (Ind. Eng. Chem. Res. 2024, 63, 9964-9975) prepared SSZ-13 molecular sieve membranes using a gel-free method, saving on the use of solvents and organic templates. Summary of the Invention

[0005] To address the aforementioned problems, the present invention aims to provide a high-performance SSZ-13 molecular sieve membrane, a method for preparing it via counter-diffusion, and its application in gas separation.

[0006] The present invention discloses a method for preparing a high-performance SSZ-13 molecular sieve membrane by counter-diffusion, the preparation steps of which are as follows:

[0007] (1) Preparation of synthetic sol: NaOH and TM-40 silica sol were dissolved in water and stirred at room temperature to obtain synthetic sol A; organic template agent N,N,N-trimethyl-1-adamantyl ammonium hydroxide (TMAdaOH) was dissolved in water and stirred at room temperature to obtain synthetic sol B;

[0008] (2) SSZ-13 molecular sieve seed crystals are coated on the outer surface of the porous alumina tube to form a seed crystal layer, which serves as a nucleation site during the crystallization reaction;

[0009] (3) Synthesis of SSZ-13 molecular sieve membrane by counter-diffusion method: The synthetic sol B obtained in step (1) is added to the inside of the porous alumina tube with a seed layer on the surface obtained in step (2), and the two ends of the porous alumina tube are sealed with polytetrafluoroethylene caps and then placed in a reaction vessel; the synthetic sol A obtained in step (1) is added to the reaction vessel and completely immersed in the porous alumina tube, crystallized at high temperature, and finally the porous alumina tube is washed, dried and calcined to remove the organic template agent, and SSZ-13 molecular sieve membrane is obtained on the outer surface of the porous alumina tube;

[0010] Porous alumina tubes serve as the carrier. The kinetic diameter of CH4 is 0.38 nm, and the kinetic diameter of N2 is 0.364 nm, while the pore size of the SSZ-13 molecular sieve membrane prepared in this invention is 0.38 nm. When the N2 / CH4 mixed gas passes through the porous alumina tube, the SSZ-13 molecular sieve membrane confines CH4, preventing it from passing through the tube wall, while N2, with a molecular size smaller than 0.38 nm, can pass through. This invention separates the gases N2 and CH4 in this way.

[0011] Further, in step (1), the molar ratio of each component in the synthesized sol A is n(SiO2):n(Na2O):n(H2O)=1:(0.1~0.4):(40~160); the molar ratio of each component in the synthesized sol B is n(TMAdaOH):n(H2O)=(1~4):(400~1600);

[0012] Furthermore, the pore size of the porous alumina tube in step (2) is 200 nm, 500 nm or 2~3 μm;

[0013] Furthermore, the crystallization time in step (3) is 1 to 48 hours, and the crystallization temperature is 160 to 190°C.

[0014] The high-separation-performance SSZ-13 molecular sieve membrane of the present invention is prepared by the above method.

[0015] The high-performance SSZ-13 molecular sieve membrane described in this invention can be well applied in the separation of N2 / CH4.

[0016] This invention proposes a counter-diffusion crystallization strategy, which involves introducing an organic template agent solution and a silicon source solution onto opposite sides of a porous alumina tube, successfully synthesizing an SSZ-13 molecular sieve membrane to achieve efficient separation of N2 from CH4. Compared to the traditional hydrothermal synthesis method, this method requires only 7.5 wt% of the organic template agent solution. Furthermore, the unreacted organic template agent aqueous solution within the porous alumina tube can be recycled and reused, further improving raw material utilization. The optimized SSZ-13 molecular sieve membrane exhibits excellent N2 / CH4 separation performance.

[0017] The beneficial effects of this invention are as follows:

[0018] This invention successfully synthesized SSZ-13 molecular sieve membranes on alumina tubes via a counter-diffusion method, exhibiting excellent separation performance. The method provided by this invention significantly reduces the use of organic template agents, and the unreacted organic template agent solution within the support tube can be recycled and reused, further improving raw material utilization, reducing manufacturing costs, and minimizing pollution.

[0019] The relevant test conditions and methods involved in this invention are as follows:

[0020] Scanning electron microscopy (SEM) testing: The morphology of the prepared membrane samples was characterized using a Hitachi Regulus 8100 high-resolution scanning electron microscope.

[0021] X-ray electron diffraction (XRD) test: The structure of the prepared film sample was characterized using a Rigaku MiniFlex 600 desktop X-ray diffractometer.

[0022] The gas separation test was performed using the Wicke-Kallenbach Technique apparatus (Angew. Chem. Int. Ed. 2006, 45, 7053-7056). The flow rates of N2, CH4 and carrier gas Ar were controlled by a mass flow controller. The feed gas permeating the membrane was purged by the carrier gas and entered the gas chromatograph. The contents of different gases were measured to ultimately determine the separation effect.

[0023] The gas permeation flux (Pi) can be calculated using formula (1):

[0024] (1)

[0025] Where Ni (mol s) -1 ) is the permeation flow rate of gas component i, Δpi (Pa) is the pressure difference across the membrane of component i, and A (m 2 ) is the effective area of ​​the membrane;

[0026] The separation factor (αi / j) for gas separation can be calculated using formula (2):

[0027] (2)

[0028] Where i and j represent two components in the mixture.

[0029] Gas chromatography (GC) analysis: Shimadzu GC2014; column temperature: 50℃; detector: TCD; the gas mixture consisted of N2 and CH4 in a 1:1 volume ratio. Attached Figure Description

[0030] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0031] Figure 1 The XRD patterns of the SSZ-13 molecular sieve membranes in Examples 1-6 are shown.

[0032] Figure 2 SEM images of the SSZ-13 molecular sieve membranes in Examples 1-6;

[0033] Figure 3 The graphs show the N2 / CH4 separation performance of the SSZ-13 molecular sieve membranes in Examples 1-5.

[0034] Figure 4This is a comparison chart of the N2 / CH4 separation performance of the SSZ-13 molecular sieve membrane in Example 3 and Comparative Example 1. Detailed Implementation

[0035] The present invention will be further described in detail below with reference to embodiments, but the implementation methods and protection scope of the present invention are not limited thereto.

[0036] Example 1

[0037] (1) Preparation of synthetic sol: 1.5g of NaOH and 26.8g of TM-40 silica sol were added to 241.6g of water and dissolved. The mixture was stirred for 8 hours to obtain synthetic sol A. The molar ratio of each component was n(SiO2):n(Na2O):n(H2O)=1:0.1:80. In addition, 1.2g of TMAdaOH was added to 18.8g of water and stirred at room temperature for 8 hours to obtain synthetic sol B. The molar ratio of TMAdaOH:n(H2O)=1:800.

[0038] (2) SSZ-13 molecular sieve seed crystals are coated on the outer surface of the porous alumina tube to form a seed crystal layer, which serves as a nucleation site during the crystallization reaction; the outer diameter of the porous alumina tube is 12 mm, the inner diameter is 8 mm, and the surface pore size of the porous alumina tube is 200 nm.

[0039] (3) Synthesis of SSZ-13 molecular sieve membrane by counter-diffusion method: Synthetic sol B was added into a porous alumina tube coated with a seed layer, and the two ends of the porous alumina tube were sealed with polytetrafluoroethylene caps and then placed in a reaction vessel; then synthetic sol A was added into the reaction vessel and completely immersed in the porous alumina tube, and crystallized at 180°C for 6 hours; finally, the porous alumina tube was washed, dried and calcined at 500°C for 10 hours to remove the organic template agent.

[0040] Membrane characterization:

[0041] Figure 1 Curve (b) is the XRD characterization diagram of the product. As can be seen from the figure, characteristic peaks appear at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, corresponding to... Figure 1 The peak position of the SSZ-13 standard peak in the curve (a) proves that the synthesized membrane is a pure phase SSZ-13 molecular sieve membrane; Figure 2 (a) and Figure 2 (a') is an electron microscope image of the SSZ-13 molecular sieve membrane. The image shows that the membrane surface is covered with blocky particles that are not yet fully formed. The particle size is about 1 μm and the membrane thickness is 1 μm.

[0042] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 1.

[0043] Table 1: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0044] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 1.49 0.39 3.8

[0045] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0046] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0047] Example 2

[0048] The preparation steps of the SSZ-13 molecular sieve membrane are the same as in Example 1, except that the crystallization time is changed to 12 hours.

[0049] Membrane characterization:

[0050] Figure 1 Curve (c) is the XRD characterization diagram of the product. As can be seen from the figure, characteristic peaks appear at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, and the peak intensities are significantly enhanced. Figure 1 The curve (a) shows the peak position of the SSZ-13 standard peak, proving that the synthesized membrane is a pure phase SSZ-13 molecular sieve membrane; Figure 2 (b) and Figure 2 (b') is an electron microscope image of the SSZ-13 molecular sieve membrane. It can be seen from the image that the particles on the surface of the membrane tend to dissolve gradually. The particle size is about 500 nm and the membrane thickness is 1 μm.

[0051] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 2.

[0052] Table 2: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0053] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 1.3 0.25 5.2

[0054] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0055] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0056] Example 3

[0057] The preparation steps of the SSZ-13 molecular sieve membrane are the same as in Example 1, except that the crystallization time is changed to 24 hours.

[0058] Membrane characterization:

[0059] Figure 1 Curve (d) is the XRD characterization diagram of the product. It can be seen from the figure that characteristic peaks appear clearly at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, and the peak intensity is significantly enhanced. Figure 1 The curve (a) shows the peak position of the SSZ-13 standard peak, proving that the synthesized membrane is a pure phase SSZ-13 molecular sieve membrane; Figure 2 (c) and Figure 2 (c') is an electron microscope image of the SSZ-13 molecular sieve membrane. As can be seen from the image, the bulk metastable crystals are dissolved and transformed into a more stable petal-shaped crystal morphology composed of plates. The width of the plate morphology is about 1 μm, and the membrane morphology is more compact with a thickness of 2 μm.

[0060] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 3.

[0061] Table 3: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0062] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 0.63 0.04 16.6

[0063] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0064] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0065] Example 4

[0066] The preparation steps of the SSZ-13 molecular sieve membrane are the same as in Example 1, except that the crystallization time is changed to 36 hours.

[0067] Figure 1 Curve (e) is the XRD characterization of the product. As can be seen from the figure, characteristic peaks appear clearly at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, and the peak intensities are significantly enhanced. Figure 1 The curve (a) shows the peak position of the SSZ-13 standard peak, proving that the synthesized membrane is a pure phase SSZ-13 molecular sieve membrane; Figure 2 (d) and Figure 2 (d') is an electron microscope image of the SSZ-13 molecular sieve membrane. As can be seen from the image, the crystal morphology (petal-like) and membrane thickness do not change significantly. The size is about 1 μm and the membrane thickness is 2 μm.

[0068] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 4.

[0069] Table 4: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0070] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 0.63 0.26 2.4

[0071] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0072] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0073] Example 5

[0074] The preparation steps of the SSZ-13 molecular sieve membrane are the same as in Example 1, except that the crystallization time is changed to 48 hours.

[0075] Membrane characterization:

[0076] Figure 1 Curve (f) is the XRD characterization diagram of the product. It can be seen from the figure that characteristic peaks appear clearly at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, and the peak intensities are significantly enhanced. Figure 1 The curve (a) shows the peak position of the SSZ-13 standard peak, proving that the synthesized membrane is a pure phase SSZ-13 molecular sieve membrane; Figure 2 (e) and Figure 2 (e') is an electron microscope image of the SSZ-13 molecular sieve membrane. As can be seen from the image, the crystal morphology (petal-like) and membrane thickness do not change significantly. The size is about 1 μm and the membrane thickness is 2 μm.

[0077] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 5.

[0078] Table 5: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0079] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 0.98 0.50 2.0

[0080] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0081] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0082] Comparative Example 1

[0083] (1) Preparation of synthetic sol: 1.5g of NaOH and 26.8g of TM-40 silica sol were added to 120g of water and dissolved. The mixture was stirred at room temperature for 6 hours to obtain synthetic sol A. 16g of TMAdaOH was dissolved in 110g of water and stirred at room temperature for 30min. The mixture was then added to synthetic sol A and stirred for 8 hours to obtain synthetic sol B. The molar ratio of each component was n(SiO2):n(Na2O):n(TMAdaOH):n(H2O) = 1:0.1:0.1:80.

[0084] (2) SSZ-13 molecular sieve seed crystals are coated on the outer surface of the porous alumina tube to form a seed layer, which serves as a nucleation site during the crystallization reaction. The outer diameter of the porous alumina tube is 12 mm, the inner diameter is 8 mm, and the surface pore size of the porous alumina tube is 200 nm.

[0085] (3) Synthesis of SSZ-13 molecular sieve membrane by traditional hydrothermal method: The obtained synthetic sol B and the porous alumina tube coated with seed layer were placed together in the reactor. The synthetic sol B completely immersed the porous alumina tube, and then crystallized at 180°C for 24 hours. Finally, the porous alumina tube was washed, dried and calcined at 500°C for 10 hours to remove the organic template agent.

[0086] Membrane characterization:

[0087] Figure 1 Curve (g) is the XRD characterization diagram of the product. As can be seen from the figure, characteristic peaks clearly appear at positions 2θ = 9.4, 12.8, 15.9, 17.5, 20.4, 25.7, and 30.7, corresponding to... Figure 1 The curve (a) shows the elution position of the SSZ-13 standard peak, proving that the synthesized membrane is a pure-phase SSZ-13 molecular sieve membrane. The membrane synthesized by the counter-diffusion method is thinner (2μm), while the membrane generated by the traditional hydrothermal synthesis method in the comparative example is thicker (3μm). Generally speaking, the thicker the membrane layer, the lower the permeation flux, so there will be a difference in permeation flux. Figure 2 (f) and Figure 2 (f') is an electron microscope image of the SSZ-13 molecular sieve membrane. The image shows that the crystal morphology is petal-shaped, with a size of about 1 μm and a membrane thickness of 3 μm.

[0088] The separation performance of the membrane against N2 / CH4 gas was tested at 2 bar and 25°C. The results are shown in Table 6.

[0089] Table 6: N2 / CH4 gas flux and separation factor at 2 bar pressure

[0090] <![CDATA[N2 Permeance]]> <![CDATA[CH4 Permeance]]> <![CDATA[N2 / CH4 separation factor]]> 0.1 0.01 14.5

[0091] Flux is the volume of gas that permeates per unit time per unit membrane area.

[0092] CH4 flux unit: 1*10 -8 mol / (m 2 s Pa).

[0093] Figure 1 The images show the XRD patterns of the SSZ-13 molecular sieve membranes in Examples 1-6. SSZ-13 molecular sieve membranes with different crystallization times were prepared by the counter-diffusion method. The XRD diffraction patterns show that the counter-diffusion method can successfully prepare SSZ-13 molecular sieve membranes.

[0094] Figure 2 The images show SEM images of the SSZ-13 molecular sieve membranes in Examples 1-6, demonstrating that continuous and defect-free SSZ-13 molecular sieve membranes can be successfully prepared by reacting for 24 hours via the counter-diffusion method.

[0095] Figure 3 The figures show the N2 / CH4 separation performance of the SSZ-13 molecular sieve membranes in Examples 1-5. The results indicate that the SSZ-13 molecular sieve membranes prepared by the counter-diffusion method after 24 hours of reaction possess an excellent N2 / CH4 separation factor (16.6) and a good N2 permeation flux [0.63*10]. -8 mol / (m 2 s Pa)];

[0096] Figure 4 This is a comparison of the N2 / CH4 separation performance of the SSZ-13 molecular sieve membranes in Example 3 and Comparative Example 1. The results show that the SSZ-13 molecular sieve membrane prepared by the counter-diffusion method has a higher gas flux [0.63*10] than that prepared by the traditional hydrothermal method. -8 mol / (m 2 sPa)>0.1*10 -8 mol / (m 2 [s Pa)] and considerable gas separation capacity (16.6>14.5).

[0097] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A method for preparing a high-performance SSZ-13 molecular sieve membrane by counter-diffusion, comprising the following steps: (1) Preparation of synthetic sol: NaOH and TM-40 silica sol were dissolved in water and stirred at room temperature to obtain synthetic sol A; organic template agent N,N,N-trimethyl-1-adamantyl ammonium hydroxide (TMAdaOH) was dissolved in water and stirred at room temperature to obtain synthetic sol B; (2) SSZ-13 molecular sieve seed crystals are coated on the outer surface of the porous alumina tube to form a seed crystal layer, which serves as a nucleation site during the crystallization reaction; (3) Synthesis of SSZ-13 molecular sieve membrane by counter-diffusion method: The synthetic sol B obtained in step (1) is added to the inside of the porous alumina tube with a seed layer on the surface obtained in step (2), and the two ends of the porous alumina tube are sealed with polytetrafluoroethylene caps and then placed in a reaction vessel; the synthetic sol A obtained in step (1) is added to the reaction vessel and completely immersed in the porous alumina tube, crystallized at high temperature, and finally the porous alumina tube is washed, dried and calcined to remove the organic template agent, thereby obtaining SSZ-13 molecular sieve membrane on the outer surface of the porous alumina tube.

2. The method for preparing a high-separation-performance SSZ-13 molecular sieve membrane by counter-diffusion as described in claim 1, characterized in that: In step (1), the molar ratio of each component in the synthesized sol A is n(SiO2):n(Na2O):n(H2O)=1:(0.1~0.4):(40~160); the molar ratio of each component in the synthesized sol B is n(TMAdaOH):n(H2O)=(1~4):(400~1600).

3. The method for preparing a high-separation-performance SSZ-13 molecular sieve membrane by counter-diffusion as described in claim 1, characterized in that: The pore size of the porous alumina tube in step (2) is 200nm, 500nm or 2~3μm.

4. The method for preparing a high-separation-performance SSZ-13 molecular sieve membrane by counter-diffusion as described in claim 1, characterized in that: The crystallization time in step (3) is 1 to 48 hours, and the crystallization temperature is 160 to 190°C.

5. A high-performance SSZ-13 molecular sieve membrane, characterized in that: It is prepared by the preparation method described in any one of claims 1 to 4.

6. The application of the high separation performance SSZ-13 molecular sieve membrane as described in claim 5 in gas separation.

7. The application of the high-separation-performance SSZ-13 molecular sieve membrane as described in claim 6 in gas separation, characterized in that: Used to separate N2 and CH4.

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