Acetylene selective hydrogenation catalyst based on strong metal-carrier interaction regulation and preparation method and application thereof
By using palladium metal catalysts supported on iron oxide doped with alkali metals and/or alkaline earth metals, the problem of palladium single-atom aggregation in acetylene selective hydrogenation catalysts at high temperatures was solved, achieving highly active and selective acetylene hydrogenation reactions at medium and low temperatures, with good economic efficiency and stability.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2026-03-27
- Publication Date
- 2026-05-12
AI Technical Summary
Existing selective hydrogenation catalysts for acetylene are prone to palladium single-atom aggregation at high temperatures, which affects the reaction conversion rate and selectivity. At the same time, the preparation process is complex and costly, making it difficult to achieve high activity and high selectivity at medium and low temperatures.
Using iron oxide doped with alkali metals and/or alkaline earth metals as a support, palladium metal catalysts are loaded and prepared by deposition precipitation and impregnation-calcination methods. This forms a strong metal-support interaction, reduces the temperature at which the SMSI effect occurs, and improves the dispersibility and utilization of active components.
This catalyst exhibits high activity and selectivity in the selective hydrogenation of acetylene at medium and low temperatures, with good catalyst stability, low cost, and suitability for large-scale production.
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Abstract
Description
Technical Field
[0001] This invention relates to the field of selective hydrogenation technology for acetylene, and more specifically, to a selective hydrogenation catalyst for acetylene based on strong metal-support interaction regulation, its preparation method, and its application. Background Technology
[0002] Ethylene plays a central role in the petrochemical industry. It is not only a crucial raw material for producing various plastics but also a key indicator of a country's chemical industry level. However, in the process of producing ethylene through high-temperature cracking of petroleum hydrocarbons, a small amount of acetylene inevitably gets mixed in. Although the content of acetylene is very low, its destructive power is extremely high: it can easily cause reactor overheating and poison the catalysts in subsequent polyethylene production processes. Therefore, industrially, the acetylene content in ethylene must be strictly controlled below 5 ppm to ensure stable production. To remove this acetylene, many selective hydrogenation catalysts have been developed both domestically and internationally. These catalysts include metals from Group VIII (such as palladium, platinum, nickel, cobalt, and iron) or Group IB (such as copper and gold). Among them, palladium (Pd) has always been a hot topic in research and application due to its excellent hydrogenation activity. However, due to the high activity of Pd, it may continue to hydrogenate ethylene to ethane during the reaction, or even trigger the polymerization of low-carbon compounds to produce the byproduct "green oil," leading to a decrease in the final ethylene selectivity. Therefore, researchers devised a method: to "isolate" the spacing between Pd atoms, forming a single-atom catalyst, which could effectively suppress side reactions and significantly improve the selectivity for ethylene. However, this approach is not easy to implement; precise control of synthesis conditions is required, which tests technology and increases costs. Moreover, while pursuing ultimate selectivity, it is often difficult to balance the economy and reactivity of the catalyst.
[0003] Strong metal-support interaction (SMSI) was discovered by Tauster et al. in their study of platinum group metal (Pt, Pd, Ru, Rh, Ir, Os) catalysts supported on TiO2. They found that after high-temperature reduction treatment at 500℃, the adsorption of H2 and CO molecules by the catalyst decreased sharply, even approaching zero. Simultaneously, when the SMSI effect occurs, in addition to the change in adsorption capacity, the sample also exhibits the following characteristics: metal particles are encapsulated by the support, electron transfer occurs between the metal and the support, and the above three characteristics are completely reversible after treatment in an oxidizing atmosphere. The metal in the above SMSI effect is generally in a particulate state. SMSI can also occur in metals existing in a single-atom state, but this requires extremely high treatment temperatures. For example, the SMSI effect in Pt1-CeO2 requires treatment at 600℃ for Pt single atoms. However, due to the excessively high treatment temperature, the single atoms are likely to agglomerate and become deactivated, affecting the conversion rate and selectivity of subsequent reactions. Therefore, reducing the temperature at which the SMSI effect occurs is an urgent problem to be solved. Summary of the Invention
[0004] The purpose of this invention is to overcome the aforementioned defects in the prior art and provide a selective hydrogenation catalyst for acetylene based on strong metal-support interaction, its preparation method, and its application. This catalyst has a low palladium loading and a high metal atom utilization rate. Its iron oxide support, doped with alkali metals and / or alkaline earth metals, has reducing properties and easily forms strong metal-support interactions. When applied to the selective hydrogenation reaction of acetylene, it can efficiently catalyze the selective production of ethylene from acetylene under medium and low temperature conditions. It has the advantages of high activity, high selectivity, and catalytic stability. At the same time, the preparation process is simple and easy to scale up, showing good application prospects.
[0005] To achieve the above objectives, the technical solution of the present invention is as follows:
[0006] A selective hydrogenation catalyst for acetylene based on strong metal-support interaction regulation, the catalyst comprising a support and an active component supported on the support; wherein the support is iron oxide doped with alkali metal and / or alkaline earth metal; the active component is palladium; based on the total mass of the catalyst, the palladium loading is 0.01% to 10% of the catalyst mass, preferably 0.05% to 5%; based on the total mass of the support, the alkali metal and / or alkaline earth metal loading is 1% to 20% of the support mass, preferably 1% to 15%.
[0007] Optionally, the iron oxide doped with alkali metals and / or alkaline earth metals is selected from at least one of sodium-doped iron oxide, potassium-doped iron oxide, magnesium-doped iron oxide, and calcium-doped iron oxide.
[0008] Optionally, the palladium is dispersed on a support in at least one of the forms of nanoparticles, nanoclusters, and atomic-level forms.
[0009] Optionally, the particle size of the iron oxide doped with alkali metals and / or alkaline earth metals is 10 nm to 5000 nm. Preferably, the particle size is 50 nm to 4000 nm; more preferably, the particle size is 60 nm to 3800 nm; even more preferably, the particle size is 80 nm to 3000 nm; and most preferably, the particle size is 100 nm to 3000 nm.
[0010] Optionally, the specific surface area of the iron oxide doped with alkali metals and / or alkaline earth metals is 15 m². 2 / g~300m 2 / g, preferably 50m 2 / g~300m 2 / g.
[0011] Optionally, the palladium has a particle size of 0.3 nm to 100 nm, preferably 0.3 nm to 50 nm.
[0012] This invention also discloses a method for preparing an acetylene selective hydrogenation catalyst based on strong metal-support interaction as described above, comprising the following steps: S1. Prepare iron oxide doped with alkali metals and / or alkaline earth metals; S2. Dissolve the palladium metal precursor in a solvent to obtain a mixture; S3. Add the iron oxide doped with alkali metal and / or alkaline earth metal to the mixture, and then disperse, filter, wash and dry it in sequence to obtain the catalyst precursor. S4. The catalyst precursor is calcined in an air atmosphere to obtain the catalyst.
[0013] Optionally, in step S1, the method for preparing iron oxide doped with alkali metals and / or alkaline earth metals includes: preparing iron oxide doped with alkali metals and / or alkaline earth metals by precipitation deposition followed by calcination; wherein the calcination temperature is 100℃~1000℃, preferably 200℃~800℃; and the calcination time is 1h~48h.
[0014] Optionally, in step S1, the method for preparing the iron oxide doped with alkali metals and / or alkaline earth metals includes: dissolving ferric nitrate in ultrapure water, simultaneously adding the obtained ferric nitrate solution and alkali metal salt solution and / or alkaline earth metal salt solution to a sodium carbonate solution, and sequentially filtering, washing, drying and calcining to obtain a carrier.
[0015] Optionally, in step S2, the palladium metal precursor includes one or more of sodium tetrachloropalladate, palladium acetylacetonate, palladium chloride, palladium tetraaminonitrate, palladium nitrate, and palladium acetate.
[0016] Optionally, in step S2, the concentration of the palladium metal precursor in the mixture is 0.1% to 15%.
[0017] Optionally, in step S2, the solvent is water or benzene.
[0018] Optionally, step S3 specifically includes: drying iron oxide doped with alkali metals and / or alkaline earth metals at 40℃~1000℃, adding the dried iron oxide doped with alkali metals and / or alkaline earth metals to a mixed solution, and sequentially dispersing, filtering, washing, and drying at 40℃~300℃ for 1h~48h to obtain a catalyst precursor.
[0019] Optionally, in step S4, the roasting temperature is 100℃~1000℃; the roasting time is 1h~48h; preferably, the roasting temperature is 100℃~900℃; the roasting time is 1h~40h; more preferably, the roasting temperature is 200℃~800℃; the roasting time is 1h~30h.
[0020] The present invention also discloses an acetylene selective hydrogenation catalyst based on strong metal-support interaction as described above, or the application of the catalyst prepared by the preparation method described above in the selective hydrogenation of acetylene to ethylene.
[0021] Optionally, the catalyst is subjected to a reduction treatment before application; the reduction treatment is carried out under hydrogen conditions with a concentration of 1% to 100%; the temperature of the reduction treatment is 100℃ to 900℃, preferably 100℃ to 600℃, and the time of the reduction treatment is 1h to 24h.
[0022] Optionally, the reaction conditions for the selective hydrogenation of acetylene to ethylene include: using ethylene, acetylene, and hydrogen as raw materials, carrying out the reaction in a medium-low pressure fixed-bed reactor, with a reaction temperature of 20℃~500℃, a reaction pressure of 0.1MPa~5MPa, and the internal standard in the reaction gas being 1%~40% by volume of inert gas argon or nitrogen.
[0023] Implementing the embodiments of the present invention will have the following beneficial effects: The palladium metal catalyst supported on iron oxide doped with alkali metals and / or alkaline earth metals provided by this invention uses palladium as the active component and iron oxide doped with alkali metals and / or alkaline earth metals as the support. Palladium is dispersed on the support in at least one of the forms of nanoparticles, nanoclusters, and atomic-level forms. The preparation method is simple, with low palladium loading and high metal atom utilization. Its support has a high specific surface area and good adsorption performance, realizing the SMSI effect at a lower temperature. It can be applied to the selective hydrogenation reaction of acetylene under relatively mild conditions, and has the advantages of high activity, high selectivity, and catalyst stability during the reaction.
[0024] The palladium metal catalyst supported on iron oxide doped with alkali metals and / or alkaline earth metals provided by this invention has low material cost, stable catalyst structure during reaction, and is easy to reuse for a long time. It has significant technical and economic benefits and is conducive to promotion.
[0025] This invention achieves the construction of SMSI in a catalyst system in a low-cost, simple, and efficient manner. It introduces the noble metal palladium and an iron oxide support doped with alkali metals and / or alkaline earth metals through deposition precipitation and impregnation-calcination methods to form a catalyst. Specifically, iron oxide doped with alkali metals and / or alkaline earth metals, with a large specific surface area, is selected as the support to improve the dispersibility of the active components in the catalyst, thus ensuring its stability. The iron oxide doped with alkali metals and / or alkaline earth metals exhibits the SMSI effect at a lower temperature than pure iron oxide, which is more conducive to low-temperature SMSI construction. Furthermore, this invention uses palladium, a noble metal with excellent catalytic hydrogenation activity, and optimizes the calcination temperature and time, as well as the palladium loading, through continuous experimentation. This results in a catalyst with good dispersibility of active components, high utilization rate, and stable catalytic performance. The preparation method of this invention is simple, easy to operate, and suitable for large-scale production, thus overcoming the shortcomings of existing metal catalyst preparation processes and low selectivity in the selective hydrogenation of acetylene. Attached Figure Description
[0026] Figure 1 This is an electron microscope image of the palladium metal catalyst prepared in Example 1.
[0027] Figure 2 The graph shows the performance evaluation results of application example 2. Detailed Implementation
[0028] The present invention will be further described below with reference to specific embodiments, but this does not limit the present invention in any way.
[0029] Example 1 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a potassium-doped iron oxide support and an active component palladium supported on the support.
[0030] Based on the total mass of the catalyst, the palladium loading was 4% of the catalyst mass; based on the total mass of the support, the potassium loading was 5% of the support mass. The support particle size was 400 nm. The palladium particle size was 5 nm.
[0031] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. Preparation of the carrier: Ferric nitrate was dissolved in ultrapure water by precipitation deposition. The resulting ferric nitrate solution and potassium nitrate solution were added to sodium carbonate solution at the same time. The solution was then filtered, washed, dried and calcined in sequence. The calcination temperature was 500℃ and the calcination time was 24h to obtain the carrier.
[0032] S2. Dissolve the Pd(NO3)2(NH3)4 precursor in water to obtain a mixed solution with a concentration of 0.5%.
[0033] S3. The support is dried at 200℃ for 12 hours. The dried support is added to the mixture and dispersed, filtered and washed in sequence. It is then dried at 80℃ for 5 hours to obtain the catalyst precursor.
[0034] S4. The catalyst precursor was calcined in air at a heating rate of 5℃ / min, at a temperature of 700℃, and for 5 hours. After natural cooling, the sample was removed and designated CAT-1. Characterization by electron microscopy yielded the following results: Figure 1 As shown.
[0035] Example 2 The only difference between this embodiment and Embodiment 1 is that the Pd precursor used is changed to Na2PdCl4 precursor. In step S4, the calcination temperature is 500℃, denoted as CAT-2.
[0036] Example 3 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a sodium-doped iron oxide support and an active component palladium supported on the support.
[0037] Based on the total mass of the catalyst, the palladium loading was 3% of the catalyst mass; based on the total mass of the support, the sodium loading was 5% of the support mass. The support particle size was 200 nm. The palladium particle size was 10 nm.
[0038] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. The carrier was prepared according to the preparation method of Example 1.
[0039] S2. Dissolve the Pd(acac)2 precursor in benzene solvent to obtain a 5% concentration mixture.
[0040] S3. The support is dried at 200℃ for 24 hours. The dried support is added to the mixture and dispersed, filtered and washed in sequence. It is then dried at 100℃ for 12 hours to obtain the catalyst precursor.
[0041] S4. The catalyst precursor was calcined in air at a heating rate of 2℃ / min, a calcination temperature of 300℃, and a calcination time of 5h. After natural cooling, the sample was taken out and labeled CAT-3.
[0042] Example 4 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a calcium-doped iron oxide support and an active component palladium supported on the support.
[0043] Based on the total mass of the catalyst, the palladium loading was 5% of the catalyst mass; based on the total mass of the support, the calcium loading was 20% of the support mass. The support particle size was 300 nm. The palladium particle size was 1 nm.
[0044] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. The carrier was prepared according to the preparation method of Example 1.
[0045] S2. Dissolve the PdCl2 precursor in water to obtain a 0.1% mixture.
[0046] S3. The support is dried at 300℃ for 6 hours. The dried support is added to the mixture and then dispersed, filtered, and washed. The mixture is then dried at 80℃ for 8 hours to obtain the catalyst precursor.
[0047] S4. The catalyst precursor was calcined in air at a heating rate of 10℃ / min, a calcination temperature of 500℃, and a calcination time of 5h. After natural cooling, the sample was taken out and labeled CAT-4.
[0048] Example 5 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a magnesium-doped iron oxide support and an active component palladium supported on the support.
[0049] Based on the total mass of the catalyst, the palladium loading is 7% of the catalyst mass; based on the total mass of the support, the magnesium loading is 20% of the support mass.
[0050] The carrier has a particle size of 1000 nm. The palladium has a particle size of 1 nm.
[0051] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. The carrier was prepared according to S1 of Example 1.
[0052] S2. Dissolve the PdCl2 precursor in water to obtain a 5% concentration mixture.
[0053] S3. The support is dried at 200℃ for 48 hours. The dried support is added to the mixture and dispersed, filtered, and washed in sequence. It is then dried at 120℃ for 10 hours to obtain the catalyst precursor.
[0054] S4. Prepare according to S4 of Example 1, and take out the sample after natural cooling. It is denoted as CAT-5.
[0055] Example 6 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a magnesium-doped iron oxide support and an active component palladium supported on the support.
[0056] Based on the total mass of the catalyst, the palladium loading was 1% of the catalyst mass; based on the total mass of the support, the magnesium loading was 1% of the support mass.
[0057] The particle size of the carrier is 100 nm, and the particle size of palladium is 10 nm.
[0058] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. The carrier was prepared according to the preparation method of Example 1.
[0059] S2. Dissolve the Na2PdCl4 precursor in water to obtain a 5% concentration mixture.
[0060] S3. The support is dried at 600℃ for 3 hours. The dried support is added to the mixture and then dispersed, filtered, and washed. The mixture is then dried at 150℃ for 10 hours to obtain the catalyst precursor.
[0061] S4. The catalyst precursor was calcined in air at a heating rate of 10℃ / min, at a temperature of 800℃, and for 16 hours. After natural cooling, the sample was taken out and designated as CAT-6.
[0062] Example 7 The selective hydrogenation catalyst for acetylene based on strong metal-support interaction in this embodiment consists of a support and an active component supported on the support; wherein the support is sodium-doped iron oxide; the active component is palladium; based on the total mass of the catalyst, the palladium loading is 6% of the catalyst mass; based on the total mass of the support, the sodium loading is 10% of the support mass.
[0063] The carrier has a particle size of 200 nm, and the palladium has a particle size of 10 nm.
[0064] The preparation method of the acetylene selective hydrogenation catalyst based on strong metal-support interaction in this embodiment includes the following steps: S1. The carrier was prepared according to the preparation method of Example 1.
[0065] S2. Dissolve the Na2PdCl4 precursor in water to obtain a 0.5% concentration mixture.
[0066] S3. Dry the support at 600℃ for 1 hour, add the dried support to the mixture, and then disperse, filter, and wash it in sequence. Dry it at 60℃ for 20 hours to obtain the catalyst precursor.
[0067] S4. The catalyst precursor was calcined in air at a heating rate of 10℃ / min, at a temperature of 600℃, and for 10 hours. After natural cooling, the sample was removed and designated as CAT-7.
[0068] Example 8 The only difference between this embodiment and Example 1 is that the calcination temperature is 200℃ and the catalyst is designated as CAT-8.
[0069] Example 9 The only difference between this embodiment and Example 1 is that the calcination temperature is 800℃ and the catalyst is designated as CAT-9.
[0070] Example 10 The only difference between this embodiment and Example 1 is that the precursor is replaced with Pd(NO3)2 and the catalyst is designated as CAT-10.
[0071] Example 11 The only difference between this embodiment and Example 1 is that the precursor is changed to Pd(OAc)2 and the catalyst is designated as CAT-11.
[0072] Example 12 The only difference between this embodiment and Example 1 is that, based on the total mass of the catalyst, the palladium loading is 1% of the catalyst mass, and the catalyst is designated as CAT-12.
[0073] Comparative Example 1 The only difference between this comparative example and Example 1 is that, based on the total mass of the catalyst, the palladium loading is 20% of the catalyst mass, denoted as CAT-Comparative-1.
[0074] Comparative Example 2 The only difference between this comparative example and Example 1 is that the carrier used is an iron oxide carrier, that is, an iron oxide carrier without alkali metal doping, denoted as CAT-Comparative-2.
[0075] Comparative Example 3 The only difference between this comparative example and Example 1 is that, based on the total mass of the carrier, the potassium loading is 25% of the carrier mass, denoted as CAT-Comparative-3.
[0076] Application Example 1 The catalyst prepared above was subjected to reduction treatment; the reduction treatment was carried out under a hydrogen atmosphere with a concentration of 5%; the reduction treatment temperature was 400℃ and the reduction treatment time was 3h.
[0077] Performance was evaluated in a medium-low pressure fixed bed reactor. 20 mg of the prepared palladium metal catalyst and 200 mg of 300-mesh quartz sand were added to the reaction tube and mixed thoroughly. The volume fractions of the feed gas components were: 2% acetylene, 20% hydrogen, 40% ethylene, and argon as the internal standard. The reaction pressure was 0.1 MPa, and the reaction temperature was 120 °C. Specific reaction results are shown in Table 1 (selectivity is negative, i.e., excessive hydrogenation).
[0078] Table 1 Catalytic performance of selective hydrogenation of acetylene to ethylene in the examples and comparative examples
[0079] Application Example 2 The catalyst of Example 1 was subjected to reduction treatment; the reduction treatment was carried out under a hydrogen atmosphere with a concentration of 5%; the reduction treatment temperature was 300°C and the reduction treatment time was 5 hours.
[0080] Performance evaluation was conducted in a medium-low pressure fixed-bed reactor. 20 mg of the prepared palladium metal catalyst and 200 mg of 200-mesh quartz sand were added to the reaction tube and mixed thoroughly. The feed gas composition (volume fraction) was: 2% acetylene, 20% hydrogen, 40% ethylene, with argon as the internal standard, and the reaction pressure was 0.1 MPa. Catalyst activity was tested within the range of 50–150 °C, followed by stability testing at 80 °C. The results are as follows: Figure 2 It is evident that this catalyst exhibits high activity, ethylene selectivity, and good stability.
[0081] In summary, this invention utilizes iron oxide doped with alkali metals and / or alkaline earth metals, which has a large specific surface area, certain alkalinity, and adsorption capacity, as a support via electrostatic adsorption. It introduces palladium, a noble metal with excellent catalytic hydrogenation activity, into the support. Through continuous experimentation and optimization of calcination temperature and time, and reasonable control of the type and loading of palladium metal precursors, the resulting catalyst exhibits characteristics such as low loading of active components, good dispersibility, high metal atom utilization, and stability. Applied to the selective hydrogenation of acetylene to ethylene, it can efficiently catalyze ethylene production under relatively mild conditions, demonstrating high activity, high selectivity, and catalyst stability in the acetylene semi-hydrogenation reaction.
[0082] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of the patent application. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these all fall within the scope of protection of the present invention. Therefore, the scope of protection of this patent should be determined by the appended claims.
Claims
1. A selective hydrogenation catalyst for acetylene based on strong metal-support interaction regulation, characterized in that, The catalyst is composed of a support and an active component supported on the support; The carrier is iron oxide doped with alkali metals and / or alkaline earth metals; the active component is palladium. Based on the total mass of the catalyst, the palladium loading is 0.01% to 10% of the catalyst mass; Based on the total mass of the carrier, the loading of alkali metals and / or alkaline earth metals is 1% to 20% of the carrier mass.
2. The selective acetylene hydrogenation catalyst based on strong metal-support interaction regulation according to claim 1, characterized in that, The iron oxide doped with alkali metals and / or alkaline earth metals is selected from at least one of sodium-doped iron oxide, potassium-doped iron oxide, magnesium-doped iron oxide, and calcium-doped iron oxide; the palladium is dispersed on the support in at least one of nanoparticles, nanoclusters, and atomic-level forms.
3. The selective acetylene hydrogenation catalyst based on strong metal-support interaction regulation according to claim 1, characterized in that, The iron oxide doped with alkali metals and / or alkaline earth metals has a particle size of 10 nm to 5000 nm; the specific surface area of the iron oxide doped with alkali metals and / or alkaline earth metals is 15 m². 2 / g~300m 2 / g; The palladium has a particle size of 0.3 nm to 100 nm.
4. A method for preparing an acetylene selective hydrogenation catalyst based on strong metal-support interaction as described in any one of claims 1-3, characterized in that, Includes the following steps: S1. Prepare iron oxide doped with alkali metals and / or alkaline earth metals; S2. Dissolve the palladium metal precursor in a solvent to obtain a mixture; S3. Add the iron oxide doped with alkali metal and / or alkaline earth metal to the mixture, and then disperse, filter, wash and dry it in sequence to obtain the catalyst precursor. S4. The catalyst precursor is calcined in an air atmosphere to obtain the catalyst.
5. The preparation method according to claim 4, characterized in that, In step S1, the method for preparing iron oxide doped with alkali metals and / or alkaline earth metals includes: preparing iron oxide doped with alkali metals and / or alkaline earth metals by precipitation deposition followed by calcination; wherein the calcination temperature is 100℃~1000℃; and the calcination time is 1h~48h.
6. The preparation method according to claim 4, characterized in that, In step S2, the palladium metal precursor includes one or more of sodium tetrachloropalladium, palladium acetylacetonate, palladium chloride, palladium tetraaminonitrate, palladium nitrate, and palladium acetate. The solvent is water or benzene; The concentration of palladium metal precursor in the mixture is 0.1% to 15%.
7. The preparation method according to claim 4, characterized in that, In step S3, the drying temperature is 40℃~300℃; the drying time is 1h~48h. In step S4, the calcination temperature is 100℃~1000℃; the calcination time is 1h~48h.
8. The application of a selective hydrogenation catalyst for acetylene based on strong metal-support interaction as described in any one of claims 1-3, or a catalyst prepared by the preparation method as described in any one of claims 4-7, in the selective hydrogenation of acetylene to ethylene.
9. The application according to claim 8, characterized in that, The catalyst is subjected to reduction treatment before application; the reduction treatment is carried out under hydrogen conditions with a concentration of 1% to 100%; the temperature of the reduction treatment is 100℃ to 900℃; and the time of the reduction treatment is 1h to 24h.
10. The application according to claim 8, characterized in that, The reaction conditions for the selective hydrogenation of acetylene to ethylene include: a reaction temperature of 20℃ to 500℃, a reaction pressure of 0.1MPa to 5MPa, and an internal standard of 1% to 40% by volume in the reaction gas.