A nickel-based alloy catalyst, a preparation method and application thereof

Abstract

The application belongs to the technical field of catalysts, and discloses a nickel-based alloy catalyst, a preparation method and application thereof. The catalyst comprises active metal nickel and a second modifying element M, the second modifying element M is at least one of In and Ga, the active metal nickel and the second modifying element M form a nickel-based intermetallic alloy, and are loaded on the surface of a carrier; the crystal structure of the nickel-based intermetallic alloy is a body-centered cubic structure; the catalyst can be prepared in one step by using a conventional impregnation method, and can be used for dehydrogenation of low-carbon alkanes to produce alkenes; when applied to dehydrogenation of propane to produce propylene, compared with existing catalysts, not only the propylene yield is increased by more than 20%, but also the service life of the catalyst is prolonged by more than 20%, the production cost is greatly reduced, and the catalyst has a wide application prospect in industry.

Description

Technical Field

[0001] This invention belongs to the field of catalyst technology, specifically relating to a platinum-based catalyst, its preparation method, and its application. Background Technology

[0002] Propylene is an important chemical raw material, widely used in the production of bulk chemicals such as polypropylene, acrylonitrile, and propylene oxide. With the booming development of the chemical industry, traditional propylene production processes such as petroleum cracking and catalytic cracking can no longer meet the growing market demand. Therefore, in recent years, dedicated propylene production processes, represented by propane dehydrogenation (PDH), have received widespread attention. Compared with other production routes, the PDH process has advantages such as a large price difference between raw materials and products and a simple process, making it one of the most promising propylene production technologies for industrialization.

[0003] Currently, the main industrialized PDH processes are ABB Lummus's Catofin technology and UOP's Oleflex technology. These two technologies utilize chromium oxide-based and platinum-based catalysts, respectively, but both suffer from drawbacks such as significant environmental pollution, frequent or expensive catalyst regeneration, and susceptibility to carbon buildup and deactivation. Since PDH reactions typically occur at high temperatures of 600-700℃, developing catalysts with high activity, high selectivity, and high stability has become a key research focus and a major technological bottleneck in this field.

[0004] Compared to the precious metal platinum, the non-precious metal nickel (Ni) has the advantages of low price and abundant reserves, and is expected to replace nickel in PDH reactions. However, existing nickel / alumina and nickel / silica catalysts generally suffer from low selectivity and poor stability in propane dehydrogenation. For example, methane is the main byproduct on nickel / silica catalysts, and the selectivity for propylene is only ~3%. Furthermore, it deactivates rapidly during high-temperature reactions, making it difficult to apply industrially. Summary of the Invention

[0005] This invention aims to address the technical problems of low selectivity of nickel-based catalysts prepared by existing technologies in the propane dehydrogenation to propylene reaction, and the tendency for carbon deposition and metal sintering during high-temperature and regeneration processes, which affect catalyst performance. It provides a nickel-based alloy catalyst, its preparation method, and its application. By introducing a second metal atom M (indium or gallium), the interatomic spacing of nickel atoms can be effectively increased, weakening the nickel-carbon interaction and thus suppressing side reactions such as deep dehydrogenation and cracking. When used in the propane dehydrogenation to propylene process, this catalyst, by regulating the microenvironment of nickel atoms in NiM, suppresses side reactions such as carbon deposition and deep dehydrogenation, exhibiting advantages such as high propylene selectivity and good stability.

[0006] According to one aspect of the present invention, a nickel-based alloy catalyst is provided, comprising an active metal nickel and a second modifying element M, wherein the second modifying element M is at least one of In and Ga; the active metal nickel and the second modifying element M form a nickel-based intermetallic alloy and are loaded on the surface of a support; the crystal structure of the nickel-based intermetallic alloy is a body-centered cubic structure.

[0007] Furthermore, based on the mass of the carrier, the mass percentage of the active metal Ni is 0.1%-10%.

[0008] Furthermore, the molar ratio of Ni to M is (0.5-2):1.

[0009] Furthermore, the molar ratio of Ni to M is 1:1.

[0010] According to another aspect of the present invention, a method for preparing a nickel-based alloy catalyst is provided, comprising the following steps:

[0011] (1) The support is immersed in a precursor solution of Ni and M;

[0012] (2) Dry the impregnation product obtained in step (1);

[0013] (3) The product dried in step (2) is calcined in a reducing atmosphere to obtain a nickel-based intermetallic compound NiM catalyst.

[0014] Furthermore, in step (1), the precursors of Ni and M are both their nitrates, and the solvent is water.

[0015] Furthermore, in step (3), the roasting temperature is 773-973K and the time is 0.5-3 hours.

[0016] According to another aspect of the invention, an application of the above-described nickel-based alloy catalyst is provided for the dehydrogenation of low-carbon alkanes to olefins.

[0017] Furthermore, when used for propane dehydrogenation to propylene, the reaction temperature for the propane dehydrogenation reaction is 823-923 K.

[0018] The beneficial effects of this invention are:

[0019] The nickel-based alloy catalyst provided by this invention modifies the microenvironment surrounding nickel atoms by introducing a second modifying element M (indium or gallium) into nickel, increasing the interatomic spacing of nickel and weakening the nickel-carbon interaction. This effectively suppresses side reactions such as deep dehydrogenation and cracking of propane on nickel, solving the problem of low propylene selectivity in existing nickel-based catalysts. Taking the nickel-indium catalyst as an example, the propylene selectivity reaches over 91% at 873 K, and remains above 91% after 24 hours of reaction, demonstrating excellent reaction stability.

[0020] In the NiM catalyst of this invention, nickel atoms are isolated by M atoms, thus inhibiting nickel agglomeration and sintering. Furthermore, by performing oxidation regeneration and reduction treatment with 1% oxygen and hydrogen respectively after the reaction, carbon deposits on the catalyst can be effectively removed, enabling multiple reuses of the catalyst, significantly improving its service life, and solving the problem of poor stability in existing nickel-based catalysts.

[0021] The NiM catalyst provided by this invention has a simple preparation method, which is prepared in one step by conventional impregnation method and calcined in a reducing atmosphere to form a thermodynamically stable body-centered cubic nickel-based alloy. The precursor used is inexpensive and readily available, the preparation conditions are mild and controllable, and the product has high purity, making it very suitable for industrial-scale production.

[0022] The NiM catalyst of this invention is applied to the propane dehydrogenation to propylene reaction. Compared with existing catalysts, it not only increases the propylene yield by more than 20%, but also extends the catalyst life by more than 20%, significantly reducing production costs and showing broad application prospects in industry. Attached Figure Description

[0023] Figure 1 The figure shows the performance results of the nickel-indium / silicon dioxide (NiIn / SiO2) catalyst and the nickel / silicon dioxide (Ni / SiO2) catalyst in Example 1 of the present invention for the dehydrogenation of propane to propylene.

[0024] Figure 2 These are high-magnification transmission electron microscope (TEM) images of the nickel-indium / silicon dioxide (NiIn / SiO2) catalyst and the nickel / silicon dioxide (Ni / SiO2) catalyst in Example 1 of this invention. Detailed Implementation

[0025] This invention utilizes density functional theory calculations to study a series of nickel-based intermetallic compound (NiM) catalysts. The study found that introducing a second metal atom M (such as indium or gallium) can effectively increase the interatomic spacing of nickel, weakening its activation ability for carbon-hydrogen bonds, thereby suppressing side reactions such as deep dehydrogenation and cracking. Experimental results show that the nickel-indium (NiIn) catalyst with a suitable catalytic microenvironment exhibits >91% propylene selectivity in PDH reactions, far exceeding that of nickel catalysts and comparable to platinum-based catalysts. The NiM catalyst of this invention combines excellent selectivity and stability, and holds promise as a replacement for platinum-based catalysts, providing a new approach for developing high-performance PDH catalysts. Specifically:

[0026] The present invention provides a nickel-based alloy catalyst comprising active metal nickel and a second modifying element M, wherein the second modifying element M is at least one of In and Ga; the active metal nickel and the second modifying element M form a nickel-based intermetallic alloy and are loaded on the surface of a support; the crystal structure of the nickel-based intermetallic alloy is a body-centered cubic structure.

[0027] According to some preferred embodiments of the present invention, the mass percentage of active metal Ni is preferably 0.1%-10% based on the mass of the carrier.

[0028] According to some preferred embodiments of the present invention, the molar ratio of Ni to M is preferably (0.5-2):1, and most preferably 1:1.

[0029] The present invention provides a method for preparing a nickel-based alloy catalyst, comprising the following steps:

[0030] (1) The support is immersed in a precursor solution of Ni and M;

[0031] (2) Dry the impregnation product obtained in step (1);

[0032] (3) The product dried in step (2) is calcined in a reducing atmosphere to obtain a nickel-based intermetallic compound NiM catalyst.

[0033] According to some preferred embodiments of the present invention, in step (1), the precursors of Ni and M are their nitrates, and the solvent is water.

[0034] According to some preferred embodiments of the present invention, the calcination temperature in step (3) is 773-973K and the time is 0.5-3 hours.

[0035] The present invention provides an application of a nickel-based alloy catalyst for the dehydrogenation of low-carbon alkanes to olefins.

[0036] According to some preferred embodiments of the present invention, the reaction temperature of the propane dehydrogenation reaction is 823-923 K when used for propane dehydrogenation to propylene.

[0037] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to specific embodiments and accompanying drawings.

[0038] Example 1

[0039] 1. Preparation of nickel-based intermetallic compound nickel-indium catalysts:

[0040] (1) Mix 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 590 μL of 0.1 g (In) / mL In(NO3)3 aqueous solution, and dilute with deionized water to the required volume to prepare impregnation solution.

[0041] (2) Take 1g of SiO2 carrier and impregnate it with the impregnation solution prepared in step (1) in an equal volume.

[0042] (3) The impregnated support was left to stand at room temperature overnight, then dried at 353K for 12 hours, and then calcined at 873K in a 10% H2-Ar atmosphere for 1 hour to obtain a NiIn / SiO2 catalyst with SiO2 as support and Ni loading of 3wt%.

[0043] 2. Catalyst activity test:

[0044] (1) Take 200 mg of the NiIn / SiO2 catalyst prepared in step 1 and load it into a quartz tube fixed-bed reactor with an inner diameter of 8 mm and a length of 24 cm. The catalyst, which is pre-prepared into granules with a particle size of 20-40 mesh, is loaded into the quartz fixed-bed reactor. The catalyst is diluted with quartz sand particles to a total volume of 1 mL. Before the reactivity test, the catalyst is pretreated by heating it from room temperature to 873 K at a rate of 10 K / min under a 10% volume fraction H2-Ar atmosphere and holding it for 1 h.

[0045] (2) After pretreatment, a neutralizing mixture of 16% C3H8 and 16% H2 N2 was introduced into the reaction pipeline at a flow rate of 50 mL / min to carry out the propane dehydrogenation reaction under atmospheric pressure. The products were analyzed by online gas chromatography, with a flame ionization detector equipped with a Chromosorb 102 column for detecting carbon-containing compounds and a thermal conductivity detector equipped with an Al2O3 Plot column for detecting H2, N2, and other components.

[0046] 3. Catalyst regeneration test:

[0047] (1) After 24 hours of propane dehydrogenation reaction, the catalyst underwent a cooling process under the protection of N2 atmosphere (flow rate of 34 mL / min), and the temperature dropped to 773 K;

[0048] (2) Introduce a 1% O2 / N2 (40 mL / min) mixture and allow it to react for 20 minutes to remove coke;

[0049] (3) Switch the gas flow to N2 and continue for 5 minutes to replace the oxygen in the reaction tube and gas path;

[0050] (4) Switch the gas to 20% H2 / N2 (flow rate of 42 mL / min) and heat to 873 K at a heating rate of 10 °C / min, and hold for 1 hour to carry out the next propane dehydrogenation reaction.

[0051] 4. Calculate propane conversion and propylene selectivity:

[0052] Propane conversion rate (%) = (F[C3H8]) 进口 -F[C3H8] 出口 ) / F[C3H8] 进口 ×100%

[0053] Propylene selectivity (%) = F[C3H6] 出口 / (F[C3H8] 进口 -F[C3H8] 出口 )×100%

[0054] Where [F] represents the molar flow rate of each substance.

[0055] Example 2

[0056] The nickel catalyst was prepared and its activity was evaluated according to the method in Example 1, except that the impregnation solution contained only 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution, and the resulting catalyst was denoted as Ni / SiO2.

[0057] Example 3

[0058] Nickel-based intermetallic compound catalysts were prepared and their activity evaluated according to the method in Example 1, with the only difference being that the impregnation solution contained 300 μL of a 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 295 μL of a 0.1 g (In) / mL In(NO3)3 aqueous solution. The resulting catalyst was denoted as NiIn. 0.5 / SiO2.

[0059] Example 4

[0060] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the catalyst prepared by the impregnation solution containing 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 1180 μL of 0.1 g (In) / mL In(NO3)3 aqueous solution was denoted as NiIn2 / SiO2.

[0061] Example 5

[0062] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the support used was Al2O3, denoted as NiIn / Al2O3.

[0063] Example 6

[0064] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the catalyst prepared by the impregnation solution containing 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 252.5 μL of 0.1 g (Ga) / mL Ga(NO3)3 aqueous solution was denoted as NiGa / SiO2.

[0065] Example 7

[0066] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the catalyst prepared by the impregnation solution containing 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 269.3 μL of 0.1 g (Zn) / mL Zn(NO3)2 aqueous solution was denoted as NiZn / / SiO2.

[0067] Example 8

[0068] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the catalyst prepared by the impregnation solution containing 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 277.1 μL of 0.1 g (Cu) / mL Cu(NO3)2 aqueous solution was denoted as NiCu / SiO2.

[0069] Example 9

[0070] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the catalyst prepared by the impregnation solution containing 300 μL of 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 320.5 μL of 0.1 g (Mn) / mL Mn(NO3)2 aqueous solution was denoted as NiMn / SiO2.

[0071] Example 10

[0072] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the calcination temperature was 773 K under a reducing atmosphere.

[0073] Example 11

[0074] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the calcination temperature was 973 K under a reducing atmosphere.

[0075] Example 12

[0076] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the calcination time in a reducing atmosphere was 0.5 h.

[0077] Example 13

[0078] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that a reducing atmosphere was used for calcination for 3 hours.

[0079] Example 14

[0080] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the reaction temperature was 823 K.

[0081] Example 15

[0082] Nickel-based intermetallic compound catalysts were prepared and their activity was evaluated according to the method in Example 1, with the only difference being that the reaction temperature was 923 K.

[0083] Example 16

[0084] Nickel-based intermetallic compound catalysts were prepared and their activity evaluated according to the method in Example 1, with the only difference being that the impregnation solution was a mixture of 10 μL of a 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 19.6 μL of a 0.1 g (In) / mL In(NO3)3 aqueous solution. In this case, the Ni loading was 0.1%, denoted as 0.1NiIn / SiO2.

[0085] Example 17

[0086] Nickel-based intermetallic compound catalysts were prepared and their activity evaluated according to the method in Example 1, with the only difference being that the impregnation solution was a mixture of 500 μL of a 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 983.3 μL of a 0.1 g (In) / mL In(NO3)3 aqueous solution. In this case, the Ni loading was 5%, denoted as 5NiIn / SiO2.

[0087] Example 18

[0088] Nickel-based intermetallic compound catalysts were prepared and their activity evaluated according to the method in Example 1, with the only difference being that the impregnation solution was a mixture of 1000 μL of a 0.1 g (Ni) / mL Ni(NO3)2·6H2O aqueous solution and 1966.7 μL of a 0.1 g (In) / mL In(NO3)3 aqueous solution. In this case, the Ni loading was 10%, denoted as 10NiIn / SiO2.

[0089] The experimental results of Examples 1-18 above were compared to examine the influence of different parameters on the catalyst reaction performance.

[0090] (1) The effect of the introduction of In promoter in Examples 1 and 2 on catalyst activity is shown in Table 1.

[0091] Table 1 Propane conversion and propylene selectivity on different nickel-based catalysts and commercial catalysts

[0092]

[0093] From Table 1 and Figure 1 As can be seen, compared with Ni / SiO2, the NiIn / SiO2 catalyst of this invention exhibits an initial propane conversion of 12.5% ​​and a reduction to 6.5% after 24 hours at a reaction temperature of 873 K; the propylene selectivity remains above 91% throughout the reaction, demonstrating excellent propane dehydrogenation performance and regeneration stability. This indicates that introducing In into Ni / SiO2 to form a NiIn / SiO2 catalyst significantly improves the propane dehydrogenation performance of the catalyst. Figure 2 As shown in the high-magnification transmission electron microscope image, the NiIn / SiO2 catalyst exhibits a characteristic lattice spacing (0.255 nm) belonging to the body-centered cubic NiIn alloy, indicating the presence of a body-centered cubic NiIn alloy in the catalyst.

[0094] (2) The effect of the amount of In promoter introduced in Examples 1, 2, 3 and 4 on the catalyst activity. See Table 2 for specific test results.

[0095] Table 2. Propane conversion and propylene selectivity of Ni-In catalysts with different In contents.

[0096]

[0097] As shown in Table 2, the propane dehydrogenation performance of Ni-In catalysts with different molar ratios is superior to that of Ni catalysts. A peak-volcano relationship exists between the indium content and propylene yield in the Ni-In catalyst. Specifically, a low In content (In:Ni = 0.5:1) results in a lower propylene yield; increasing the In:Ni ratio to 1:1 improves the propylene yield to some extent; further increasing the In:Ni ratio to 2:1 leads to a decrease in the propylene yield. These results indicate that the In content in the Ni-In catalyst directly affects its propane dehydrogenation performance, with the optimal In:Ni ratio of 1:1 demonstrating the best propane dehydrogenation performance.

[0098] (3) The effect of the change of support on catalyst activity in Examples 1, 2 and 5 is shown in Table 3.

[0099] Table 3 Propane conversion and propylene selectivity of Ni-In catalysts with different supports

[0100]

[0101] As can be seen from the comparison in Table 3, both SiO2 and Al2O3 can achieve good selective conversion of propane to propylene when used as supports for the nickel-indium alloy catalyst. Specifically, when Al2O3 is used as the support, the initial propylene selectivity of the NiIn / Al2O3 catalyst is 42.6%, significantly higher than that of the Ni / SiO2 catalyst; when SiO2 is used as the support, the initial propylene selectivity of the NiIn / SiO2 catalyst increases to 93.5%, indicating that SiO2 is the superior support for this Ni-In catalyst.

[0102] (4) The effect of changing the modifying elements (In, Ga, Zn, Cu or Mn) in Examples 1, 6, 7, 8 and 9 on the catalyst activity. See Table 4 for specific test results.

[0103] Table 4. Propane conversion and propylene selectivity of Ni-based catalysts with different modification elements.

[0104]

[0105] As can be seen from the comparison in Table 4, the propane dehydrogenation performance of the catalyst varies with the change of the second element. Both In and Ga exhibit good selective conversion of propane. Among these, In shows the best overall propane dehydrogenation performance, indicating that both In and Ga are suitable second modifying elements, with In being the optimal one.

[0106] (5) The effect of changing the calcination temperature in reducing atmosphere on catalyst activity in Examples 1, 10 and 11. See Table 5 for specific test results.

[0107] Table 5. Effects of calcination temperature on propane conversion and propylene selectivity of Ni-In catalysts.

[0108]

[0109] As can be seen from the comparison in Table 5, changing the calcination temperature has a certain impact on the propane dehydrogenation performance of the catalyst, but its overall performance is still better than that of the Ni / SiO2 catalyst. Specifically, the catalyst exhibits superior overall performance at a calcination temperature of 873 K, indicating that 873 K is the preferred calcination temperature.

[0110] (6) The effect of changing the calcination time in reducing atmosphere on catalyst activity in Examples 1, 12 and 13. See Table 6 for specific test results.

[0111] Table 6. Effects of calcination temperature on propane conversion and propylene selectivity of Ni-In catalysts

[0112]

[0113]

[0114] As can be seen from the comparison in Table 6, changing the calcination time has a certain impact on the propane dehydrogenation performance of the catalyst, but the overall performance is still better than that of the Ni / SiO2 catalyst. Among them, the propane dehydrogenation performance of the catalyst is better when the calcination time is 1 hour, indicating that the calcination temperature of 1 hour is the preferred option.

[0115] (7) The effect of changing the reaction temperature on the catalyst activity in Examples 1, 14 and 15. See Table 7 for specific test results.

[0116] Table 7. Effects of reaction temperature on propane conversion and propylene selectivity of Ni-In catalyst.

[0117]

[0118] As can be seen from the comparison in Table 7, changing the reaction temperature has a certain impact on the propane dehydrogenation performance of the catalyst. Specifically, the propylene yield increases with increasing reaction temperature, and the propylene selectivity is always greater than 90%. The catalyst exhibits the best propane dehydrogenation performance at a reaction temperature of 873 K, indicating that 873 K is the preferred reaction temperature.

[0119] (8) The effect of changing nickel loading on catalyst activity in Examples 1, 16, 17 and 18. See Table 8 for specific test results.

[0120] Table 8. Effects of varying nickel loading on propane conversion and propylene selectivity of Ni-In catalysts.

[0121]

[0122] As can be seen from the comparison in Table 8, the nickel loading has a certain impact on the propane dehydrogenation performance of the catalyst. The propane conversion rate increases with increasing nickel loading, and the propylene selectivity is ≥92.9%, indicating that both catalysts possess excellent selective conversion capabilities for propane to propylene. Specifically, when the nickel loading is 3%, the catalyst maintains a high propane conversion rate, and the propylene yield / nickel loading ratio is higher than that of the catalysts with nickel loadings of 5% and 10%, indicating a higher utilization rate of the active nickel metal. Therefore, a nickel loading of 3% is the preferred option.

[0123] In summary, the NiM / SiO2 catalyst of the present invention has the advantages of high selectivity and high stability for propylene, and is expected to replace existing industrial catalysts in the propane dehydrogenation to propylene process, with broad prospects for industrial application.

[0124] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. The application of a nickel-based alloy catalyst in the dehydrogenation of propane to propylene, characterized in that, The nickel-based alloy catalyst comprises active metal nickel and a second modifying element In; the mass percentage of active metal nickel is 3%-10% based on the mass of the support; the molar ratio of Ni to In is (0.5-2):1; the active metal nickel and the second modifying element In form a nickel-based intermetallic alloy and are loaded on the surface of the support, which is SiO2 or Al2O3; the crystal structure of the nickel-based intermetallic alloy is a body-centered cubic structure.

2. The application of the nickel-based alloy catalyst according to claim 1 in the propane dehydrogenation to propylene, characterized in that, The molar ratio of Ni to In is 1:

1.

3. The application of the nickel-based alloy catalyst according to claim 1 in the propane dehydrogenation to propylene, characterized in that, The preparation method of this nickel-based alloy catalyst includes the following steps: (1) The support is immersed in a precursor solution of Ni and In; (2) Dry the impregnation product obtained in step (1); (3) The product dried in step (2) is calcined in a reducing atmosphere to obtain a nickel-based intermetallic compound NiIn catalyst.

4. The application of the nickel-based alloy catalyst according to claim 3 in the propane dehydrogenation to propylene, characterized in that, In step (1), the precursors of Ni and In are their nitrates, and the solvent is water.

5. The application of the nickel-based alloy catalyst according to claim 3 in the propane dehydrogenation to propylene, characterized in that, In step (3), the roasting temperature is 773-973 K and the time is 0.5-3 hours.

6. The application of the nickel-based alloy catalyst according to claim 1 in the propane dehydrogenation to propylene, characterized in that, The reaction temperature for propane dehydrogenation is 823-923 K.

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