Catalyst for preparing propylene through ethanol-acetone catalysis as well as preparation method and application of catalyst

Abstract

The invention relates to the technical field of catalysts, in particular to a catalyst for preparing propylene through ethanol-acetone catalysis and a preparation method and application of the catalyst. The preparation method of the catalyst for preparing propylene through ethanol-acetone catalysis comprises the following steps: acidifying an H-Beta zeolite molecular sieve, cooling, washing and drying to obtain a carrier; dissolving a metal salt precursor, adding the carrier, stirring, heating, drying and roasting to obtain the catalyst, the metal salt precursor is selected from one or more of acetate, acetylacetone salt, isopropanol salt, dichloro-cyclopentadienyl salt or nitrate, and metal in the metal salt precursor is selected from one or more of scandium, yttrium, zirconium, lanthanum, cerium, hafnium or niobium. According to the catalyst prepared by the invention, the conversion reaction efficiency of an ethanol-acetone mixture and the selectivity of a propylene product are remarkably improved.

Description

Technical Field

[0001] The present invention relates to the technical field of catalysts, and in particular to a catalyst for preparing propylene by catalysis of ethanol-acetone, a preparation method thereof and an application thereof. Background Art

[0002] As a key raw material in the organic chemical and petrochemical industries, propylene production capacity directly reflects the development of a country's chemical industry. Currently, propylene is primarily produced through petroleum steam cracking and catalytic cracking processes, but it can also be synthesized from fossil resources such as coal and natural gas. However, with fossil energy resources increasingly depleted, the development of new production technologies is urgently needed to achieve large-scale production increases of light olefins and alleviate the imbalance between supply and demand in the market.

[0003] In recent years, the rapid development of biofermentation and biochemical technologies has provided technical support for the conversion of biomass (particularly lignocellulose) into acetone-butanol-ethanol mixed fermentation broths. Consequently, the production of petrochemical base chemicals such as propylene using bioethanol-acetone as feedstock has become a key non-fossil-based route for the production of light olefins. This technological route not only broadens the raw material sources for light olefins and reduces dependence on petroleum resources, but also contributes to the establishment of a complete bio-chemical industry chain. Using ABE fermentation broth (an aqueous solution of acetone-butanol-ethanol) as a reactant, a study reported the production of ketones with a selectivity of up to 92% for 4-heptanone under the catalysis of a cerium-based composite oxide. Subsequently, a study reported the production of aromatic compounds, including benzene, toluene, dimethylbenzenes, and trimethylbenzenes, with a total yield of 70% under the catalysis of an acidic molecular sieve. The products were directly separated from the aqueous solution, reducing separation energy consumption. However, these methods only produce a few larger, high-carbon products, resulting in low utilization of the high-value butanol and a high cost-effectiveness.

[0004] Therefore, the technology for producing light olefins from ethanol and acetone after separating butanol from biomass fermentation broth is gaining increasing attention in academia and industry. Prior art reports have publicly reported composite molecular sieve catalysts composed of two or more components from molecular sieves such as MOR, ZSM-5, H-Beta, and SAPO-34, achieving 100% bioethanol conversion and a maximum propylene selectivity of 26.4%. Other reports have used phosphorus-modified HZSM-5 molecular sieves to catalyze ethanol reactions. Phosphorus modification reduces the number of strong acid sites and increases the number of weak acid sites, resulting in a propylene selectivity of approximately 28%. However, these technologies suffer from low propylene selectivity and low raw material utilization, limiting their widespread use. Subsequently, prior art has combined zinc-cerium oxide with H-Beta molecular sieves in a specific mass ratio to create a composite catalyst for bioethanol conversion, achieving a single-step, high selectivity of up to 50% for propylene production from bioethanol. However, existing catalysts for the conversion of fermentation broth to olefins suffer from unsatisfactory yields, poor catalyst activity stability, and easy loss of active catalyst components. Summary of the Invention

[0005] To solve the above technical problems, the present invention provides a catalyst for preparing propylene from ethanol-acetone catalysis, a preparation method thereof, and applications thereof. The catalyst not only significantly improves the utilization efficiency of the fermentation broth mixture and the selectivity of the propylene product, but also has lower production costs and less environmental impact in industrial applications.

[0006] To this end, the present invention provides the following technical solutions:

[0007] In a first aspect, the present invention provides, in an optional embodiment, a method for preparing a propylene catalyst by catalyzing ethanol-acetone, comprising the following steps:

[0008] S1: After acidifying the H-Beta zeolite molecular sieve, cooling, washing and drying are performed to obtain a carrier;

[0009] S2: dissolving the metal salt precursor, adding the support and stirring, and then heating, drying and calcining to obtain a catalyst;

[0010] In step S2, the metal salt precursor is selected from one or more of acetate, acetylacetonate, isopropoxide, dichlorobismuth salt or nitrate, and the metal in the metal salt precursor is selected from one or more of scandium, yttrium, zirconium, lanthanum, cerium, hafnium or niobium.

[0011] In the present invention, a specific acid treatment step not only removes impurities from the raw materials but also provides a large number of silanol groups for the subsequent introduction of metal active components. Furthermore, a wet impregnation method is used to uniformly load the metal active centers onto the acid-treated H-Beta zeolite molecular sieve. The metal interacts with the silanol groups of the molecular sieve to form highly dispersed and stable active centers, achieving Lewis acid (L acid) center conversion and a dehydration reaction on the silanol groups to form propylene.

[0012] Preferably, in step S1, the acidification treatment temperature is 60-120°C for 4-24 hours; and / or the acid solution used in the acidification treatment is 8-16 mol / L nitric acid; and / or the mass volume ratio of the H-Beta zeolite molecular sieve to the acid solution is 1-2:20-40; and / or the molar ratio of SiO2 to Al2O3 in the H-Beta molecular sieve is 25. The drying temperature is 80-120°C; and / or the drying time is 12-24 hours.

[0013] Preferably, in step S2, the stirring time is 2-6 hours; and / or the heating temperature is 60-90°C. The drying temperature is 80-120°C; and / or the drying time is 12 hours. The calcining temperature is 500-600°C; and / or the calcining time is 3-6 hours.

[0014] In a second aspect, the present invention provides, in an optional embodiment, a catalyst for preparing propylene by catalysis of ethanol-acetone, which is prepared by the above-mentioned preparation method.

[0015] Preferably, based on the mass of the catalyst, the mass proportion of the metal in the metal organic salt is 1-20%.

[0016] In a third aspect, the present invention provides, in an optional embodiment, a catalyst for preparing propylene from ethanol-acetone obtained by the above preparation method, or use of the above catalyst for preparing propylene from ethanol-acetone in preparing propylene from ethanol-acetone fermentation broth.

[0017] Preferably, the method for preparing propylene from ethanol-acetone fermentation broth comprises: pre-treating the catalyst for preparing propylene from ethanol-acetone with an inert gas, pressing the catalyst into tablets, and then mixing the catalyst with the ethanol-acetone fermentation broth and carrying out a catalytic reaction at 250-550° C. to obtain propylene.

[0018] Specifically:

[0019] The method for preparing propylene from ethanol-acetone fermentation broth is:

[0020] Step 1: The ethanol-acetone catalytic preparation of propylene catalyst is placed on a tablet press for tableting, and 0.2 g of the catalyst with a 20-40 mesh size is sieved out with a sieve, and then placed in the constant temperature zone of a quartz reaction tube on a fixed bed at normal pressure for pretreatment and then reaction;

[0021] Step 2: Pretreating the catalyst obtained in step 1, using nitrogen as carrier gas, a carrier gas flow rate of 20-40 mL / min, a pretreatment temperature of 350-550° C., and a pretreatment time of 1-2 hours.

[0022] Step 3: After the pretreatment, the reactant ethanol-acetone mixture is sent into the atmospheric fixed bed by injection pump. After being vaporized in the vaporization chamber under the purge of carrier gas, it enters the quartz reaction tube and reacts in the catalytic bed. The mass space velocity of ethanol-acetone is 0.5-5h -1 , the carrier gas is nitrogen, and the carrier gas flow rate is 20-40mL / min;

[0023] Step 4: The product was analyzed online by gas chromatography using a flame ionization detector (FID) coupled with a thermal conductivity detector (TCD). The GC columns were Agilent HP-PlotQ (30 m × 0.25 mm × 0.25 μm) and TDX-01 (3 mm × 2 m), respectively. Methane was used for correlation between the FID and TCD. The FID was temperature-programmed to separate the target product using the following procedure: starting at 60°C, increasing at a rate of 10°C / min to 200°C, and holding for 4 minutes. The TCD was maintained at 100°C using a constant temperature program. The conversion of the starting material and the selectivity for the target product were calculated using the area normalization method on the chromatographic workstation. A fixed-bed temperature program was used, with the reaction temperature ranging from 250-550°C.

[0024] Compared with the prior art, the present invention has one of the following beneficial effects:

[0025] 1. The present invention utilizes a specific acid treatment step to not only remove impurities from the raw materials but also provide a large number of silanol groups for the subsequent introduction of metal active components. Furthermore, a wet impregnation method is employed to uniformly load the metal active centers onto the acid-treated H-Beta zeolite molecular sieve. This significantly improves the conversion efficiency of the ethanol-acetone mixture and the selectivity of the propylene product, while also lowering production costs and minimizing environmental impact in industrial applications.

[0026] 2. The preparation method provided by the present invention has the characteristics of simple preparation process and high structural stability.

[0027] 3. The preparation method provided by the present invention can significantly improve the catalytic ability of the catalyst for the conversion reaction of the ethanol-acetone mixture after butanol separation from the biomass fermentation broth (ABE) and the selectivity of the propylene product.

[0028] 4. The catalyst provided by the present invention exhibits excellent catalyst life and cyclic stability in the reaction, providing important technical support for industrial applications. DETAILED DESCRIPTION

[0029] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with specific embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0030] In a specific embodiment of the present invention, the metal salt precursor is selected from one or more of acetate, acetylacetonate, isopropoxide, dichlorobismuth salt, or nitrate, and the metal in the metal salt precursor is selected from one or more of scandium, yttrium, zirconium, lanthanum, cerium, hafnium, and niobium. The metal salt precursor can be selected from any combination of acetate, acetylacetonate, isopropoxide, or nitrate, and scandium, yttrium, zirconium, lanthanum, cerium, hafnium, and niobium, but the present invention is not limited thereto. For example, zirconium nitrate can be used.

[0031] The technical solution of the present invention will be described below with reference to the embodiments.

[0032] Example 1

[0033] This embodiment provides a method for preparing a propylene catalyst by catalyzing ethanol-acetone, comprising the following steps:

[0034] Step 1: First, H-Beta zeolite molecular sieve (SiO2 / Al2O3 molar ratio is 25) is used as raw powder and treated with concentrated nitric acid, wherein the acid treatment conditions are: H-Beta molecular sieve and concentrated nitric acid (concentration is 10 mol / L) are mixed in a mass volume ratio of 1:20 (g / mL), and heated and stirred in a 90°C oil bath under condensation reflux conditions for 15 hours;

[0035] Step 2: Cool the mixture in step 1) to room temperature and then wash it. After washing with water until it is neutral, place it in a 90°C forced air drying oven for 12 hours.

[0036] Step 3: Place zirconium nitrate (5% by mass of zirconium in the catalyst) in a beaker containing 40 ml of water and stir thoroughly. Then, add 1 g of the Beta sample from step 2) above. Stir for 3 hours and then heat at 80°C with stirring until evaporated to dryness.

[0037] Step 4: Place the sample impregnated and evaporated in the above step 3) in a forced air drying oven at a constant temperature of 90° C. for 12 hours, and then place it in a muffle furnace and calcine it at 550° C. for 6 hours to obtain the ethanol-acetone catalytic preparation of propylene catalyst.

[0038] Examples 2-5

[0039] Examples 2-5 all provide a method for preparing a propylene catalyst by catalysis of ethanol-acetone, comprising the following steps:

[0040] The difference between Example 2 and Example 1 is that in step 3, the weight percentage of zirconium in zirconium nitrate is 1%; the difference between Example 3 and Example 1 is that in step 3, the weight percentage of zirconium in zirconium nitrate is 3%; the difference between Example 4 and Example 1 is that in step 3, the weight percentage of zirconium in zirconium nitrate is 7%; the difference between Example 5 and Example 1 is that in step 3, the weight percentage of zirconium in zirconium nitrate is 10%. The remaining steps are the same as in Example 1.

[0041] Examples 6-11

[0042] Examples 6-11 all provide a method for preparing a propylene catalyst by catalysis of ethanol-acetone, comprising the following steps:

[0043] The difference between Example 6 and Example 1 is that: in step S3, the metal precursor salt adopts scandium nitrate (based on the mass of the catalyst, the mass of scandium in scandium nitrate accounts for 5%); the difference between Example 7 and Example 1 is that: in step S3, the metal precursor salt adopts yttrium nitrate (based on the mass of the catalyst, the mass of yttrium in yttrium nitrate accounts for 5%); the difference between Example 8 and Example 1 is that: in step S3, the metal precursor salt adopts lanthanum nitrate (based on the mass of the catalyst, the mass of lanthanum in lanthanum nitrate accounts for 5%); The difference between Example 9 and Example 1 is that in step S3, the metal precursor salt is cerium nitrate (based on the mass of the catalyst, the mass proportion of cerium in cerium nitrate is 5%); the difference between Example 10 and Example 1 is that in step S3, the metal precursor salt is hafnium nitrate (based on the mass of the catalyst, the mass proportion of hafnium in hafnium nitrate is 5%); the difference between Example 11 and Example 1 is that in step S3, the metal precursor salt is niobium nitrate (based on the mass of the catalyst, the mass proportion of niobium in niobium nitrate is 5%). The remaining steps are the same as in Example 1.

[0044] Comparative Example 1

[0045] This comparative example provides a method for preparing a propylene catalyst by catalysis of ethanol-acetone, comprising the following steps:

[0046] Step 1: Zirconium nitrate (based on the mass of the catalyst, the mass percentage of zirconium in zirconium nitrate is 5%) is placed in a beaker containing 40 ml of water, stirred thoroughly, and then 1 g of SiO2 (purchased from Shanghai Aladdin, with a specific surface area of 200 cm 2 / g), stirred for 3 hours and then heated at 80 ° C with stirring until evaporated to dryness;

[0047] Step 2: Place the sample impregnated and evaporated in the above step in a forced air drying oven at a constant temperature of 90° C. for 12 hours, and then place it in a muffle furnace and calcine it at 550° C. for 6 hours to obtain an ethanol-acetone catalytic preparation of propylene catalyst.

[0048] Comparative Examples 2-3

[0049] Comparative Example 2-3 provides a method for preparing a propylene catalyst by ethanol-acetone catalysis, comprising the following steps:

[0050] The difference between Comparative Example 2 and Comparative Example 1 is that, in step 1, SiO2 is replaced by S-1 (purchased from the catalyst plant of Nankai University); the difference between Comparative Example 3 and Comparative Example 1 is that, in step 1, H-Beta zeolite molecular sieve is replaced by MCM-41 (purchased from the catalyst plant of Nankai University); the remaining steps are the same as those in Example 1.

[0051] Comparative Examples 4-6

[0052] Comparative Examples 4-6 provide a method for preparing a propylene catalyst by ethanol-acetone catalysis, comprising the following steps:

[0053] The difference between Comparative Example 4 and Example 1 is that, in step 3, zirconium nitrate (based on the mass of the catalyst, the mass of zirconium in zirconium nitrate accounts for 5%) is replaced by copper nitrate (based on the mass of the catalyst, the mass of copper in copper nitrate accounts for 5%); the difference between Comparative Example 5 and Example 1 is that, in step 3, zirconium nitrate (based on the mass of the catalyst, the mass of zirconium in zirconium nitrate accounts for 5%) is replaced by ferric nitrate (based on the mass of the catalyst, the mass of iron in ferric nitrate accounts for 5%); the difference between Comparative Example 6 and Example 1 is that, in step 3, zirconium nitrate (based on the mass of the catalyst, the mass of zirconium in zirconium nitrate accounts for 5%) is replaced by zinc nitrate (based on the mass of the catalyst, the mass of zinc in zinc nitrate accounts for 5%).

[0054] Test Example 1

[0055] The ethanol-acetone mixture prepared in Example 1 was converted into a propylene catalyst for performance evaluation. The evaluation method was as follows:

[0056] Step 1: The ethanol-acetone catalytic preparation of propylene catalyst is placed on a tablet press for tableting, and 0.2 g of the catalyst with a 20-40 mesh size is sieved out with a sieve, and then placed in the constant temperature zone of a quartz reaction tube on a fixed bed at normal pressure for pretreatment and then reaction;

[0057] Step 2: Pretreat the catalyst in step 1. During the pretreatment, nitrogen is used as the carrier gas, the carrier gas flow rate is 20 mL / min, the pretreatment temperature is 450° C., and the pretreatment time is 1 hour.

[0058] Step 3: After the pretreatment, the reactant ethanol-acetone mixture is sent into the atmospheric fixed bed by injection pump. After being vaporized in the vaporization chamber under the purge of carrier gas, it enters the quartz reaction tube and reacts in the catalytic bed. The mass space velocity of ethanol-acetone is 1h -1 , the carrier gas is nitrogen, and the carrier gas flow rate is 20 mL / min;

[0059] Step 4: The products were analyzed online by gas chromatography. The gas chromatograph employed a flame ionization detector (FID) coupled with a thermal conductivity detector (TCD). The columns were Agilent HP-PlotQ (30 m × 0.25 mm × 0.25 μm) and TDX-01 (3 mm × 2 m), respectively. Methane was used for correlation between the FID and TCD. The FID was temperature-programmed to separate the target product. The temperature ramp was as follows: 60°C, then increased at a rate of 10°C / min to 200°C, and held for 4 min. The TCD was maintained at 100°C using a constant temperature program. The conversion of the starting material and the selectivity for the target product were calculated using the area normalization method on the chromatographic workstation. A fixed-bed reaction was performed using a temperature-programmed reaction at 300°C, 350°C, 400°C, 450°C, and 500°C. The results are shown in Table 1.

[0060] Table 1 Conversion of ethanol to acetone and selectivity of propylene at different reaction temperatures

[0061]

[0062] It can be seen from Table 1 that when the reaction temperature is 350°C, the propylene selectivity of the catalyst is the highest.

[0063] Test Example 2

[0064] The catalytic effect of the catalyst for converting the ethanol-acetone mixture prepared in Example 1 and Comparative Examples 1-6 into propylene was tested. The specific method was as follows:

[0065] Step 1: The ethanol-acetone catalytic preparation of propylene catalyst is placed on a tablet press for tableting, and 0.2 g of the catalyst with a 20-40 mesh size is sieved out with a sieve, and then placed in the constant temperature zone of a quartz reaction tube on a fixed bed at normal pressure for pretreatment and then reaction;

[0066] Step 2: Pretreat the catalyst in step 1. During the pretreatment, nitrogen is used as the carrier gas, the carrier gas flow rate is 20 mL / min, the pretreatment temperature is 450° C., and the pretreatment time is 1 hour.

[0067] Step 3: After the pretreatment, the reactant ethanol-acetone mixture is sent into the atmospheric fixed bed by injection pump. After being vaporized in the vaporization chamber under the purge of carrier gas, it enters the quartz reaction tube and reacts in the catalytic bed. The mass space velocity of ethanol-acetone is 1h -1 , the carrier gas is nitrogen, and the carrier gas flow rate is 20 mL / min;

[0068] Step 4: The product was analyzed online by gas chromatography. The gas chromatograph employed a flame ionization detector (FID) coupled with a thermal conductivity detector (TCD). The columns were Agilent HP-PlotQ (30 m × 0.25 mm × 0.25 μm) and TDX-01 (3 mm × 2 m), respectively. Methane was used for correlation between the FID and TCD. The FID was temperature-programmed to separate the target product. The temperature ramp was as follows: 60°C, then increased at a rate of 10°C / min to 200°C, then held for 4 minutes. The TCD was maintained at 100°C using a constant temperature program. The conversion of the starting material and the selectivity for the target product were calculated using the area normalization method on the chromatographic workstation. The fixed-bed reaction temperature was 350°C.

[0069] The conversion rates and propylene selectivities of the catalysts of Example 1 and Comparative Examples 1-6 are shown in Table 2.

[0070] Table 2 Conversion rate and selectivity of propylene of Example 1 and Comparative Examples 1-6 catalysts

[0071] catalyst Conversion rate (%) Propylene selectivity (%) Yield (%) Example 1 53.6 67.2 36.0 Comparative Example 1 50.4 64.4 32.5 Comparative Example 2 51.4 63.1 32.4 Comparative Example 3 51.7 60.8 31.4 Comparative Example 4 40.1 20.3 8.1 Comparative Example 5 24.4 18.4 4.5 Comparative Example 6 35.7 32.7 11.7

[0072] It can be seen from Table 2 that acidification of H-Beta molecular sieve as a catalyst support can improve the conversion rate of the catalyst and the selectivity of propylene product, while transition metals such as copper, nickel, and zinc are not conducive to the production of propylene when used as active centers.

[0073] Test Example 3

[0074] The catalytic effect of the catalyst for converting the ethanol-acetone mixture prepared in Examples 1-5 into propylene was tested, and the specific method was the same as that of Test Example 2.

[0075] The conversion rates and propylene selectivities of the catalysts of Examples 1-5 are shown in Table 3.

[0076] Table 3 Conversion rate and propylene selectivity of catalysts of Examples 1-5

[0077] catalyst Conversion rate (%) Propylene selectivity (%) Yield (%) Example 1 53.6 67.2 36.0 Example 2 50.8 64.6 32.8 Example 3 52.2 65.6 34.2 Example 4 51.8 65.7 34.0 Example 5 51.5 64.8 33.4

[0078] It can be seen from Table 3 that the performance of the catalyst is optimal when the mass proportion of zirconium in zirconium nitrate exceeds 5%, that is, when the mass of metal loaded on the catalyst for converting ethanol-acetone mixture to propylene exceeds 5%.

[0079] Test Example 4

[0080] The catalytic effects of the catalysts for converting the ethanol-acetone mixture prepared in Example 1 and Examples 6-11 into propylene were tested. The specific methods were the same as those in Test Example 2.

[0081] The conversion rates and propylene selectivities of the catalysts of Example 1 and Examples 6-11 are shown in Table 4.

[0082] Table 4 Conversion rate and propylene selectivity of catalysts in Example 1 and Examples 6-11

[0083]

[0084]

[0085] It can be seen from Table 4 that when the metal is zirconium, the catalytic effect of the catalyst is the best, and the catalytic effects from best to worst are zirconium, scandium, yttrium, hafnium, cerium, niobium, and lanthanum.

[0086] Although the principles of the present invention have been described in detail above in conjunction with the preferred embodiments of the present invention, those skilled in the art should understand that the above embodiments are merely illustrative of the present invention and are not intended to limit the scope of the present invention. The details in the embodiments do not constitute a limitation on the scope of the present invention. Without departing from the spirit and scope of the present invention, any obvious changes such as equivalent transformations and simple substitutions based on the technical solution of the present invention fall within the scope of protection of the present invention.

Claims

1. A method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone, characterized in that: The following steps are involved: S1: After acidifying the H-Beta zeolite molecular sieve, cooling, washing and drying are performed to obtain a carrier; S2: dissolving the metal salt precursor, adding the support and stirring, and then heating, drying and calcining to obtain an ethanol-acetone catalytic catalyst for preparing propylene; In step S2, the metal salt precursor is selected from one or more of acetate, acetylacetonate, isopropoxide, dichlorobismuth salt or nitrate, and the metal in the metal salt precursor is selected from one or more of scandium, yttrium, zirconium, lanthanum, cerium, hafnium or niobium.

2. The method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone according to claim 1, wherein: In step S1, the acidification treatment is performed at a temperature of 60-120° C. for a time of 4-24 hours; and / or The acid solution used in the acidification treatment is 8-16 mol / L nitric acid; and / or, The mass volume ratio of the H-Beta zeolite molecular sieve and the acid solution is 1-2:20-40; and / or, The molar ratio of SiO2 to Al2O3 in the H-Beta molecular sieve is 25.

3. The method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone according to claim 1, characterized in that: In step S1, the drying temperature is 80-120°C; and / or, The drying time is 12-24 hours.

4. The method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone according to claim 1, wherein: In step S2, the stirring time is 2-6 hours; and / or, The heating temperature is 60-90°C.

5. The method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone according to claim 1, characterized in that: In step S2, the drying temperature is 80-120°C; and / or, The drying time is 12 hours.

6. The method for preparing a catalyst for preparing propylene by catalysis of ethanol and acetone according to claim 1, characterized in that: In step S2, the calcination temperature is 500-600°C; and / or, The roasting time is 3-6 hours.

7. A catalyst for preparing propylene by catalysis of ethanol and acetone, characterized in that: The product is prepared by the preparation method according to any one of claims 1 to 6.

8. The catalyst for preparing propylene by catalysis of ethanol-acetone according to claim 7, characterized in that: Based on the mass of the catalyst, the mass proportion of the metal in the metal organic salt is 1-20%.

9. Use of the catalyst for preparing propylene by catalytic ethanol-acetone obtained by the preparation method according to any one of claims 1 to 6 or the catalyst for preparing propylene by catalytic ethanol-acetone according to claim 7 or 8 in preparing propylene by ethanol-acetone fermentation broth.

10. The use according to claim 9, characterized in that The method for preparing propylene from ethanol-acetone fermentation broth is: The catalyst for preparing propylene by catalyzing ethanol-acetone is pretreated with inert gas and then tabletted. The catalyst is then mixed with ethanol-acetone fermentation liquid and subjected to catalytic reaction at 250-550° C. to obtain propylene.

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