A method for preparing an oil catalyst, the oil catalyst and an oil

Abstract

The application discloses an oil product catalyst preparation method, an oil product catalyst and an oil product, and relates to the technical field of catalysts, in particular to an oil product catalyst preparation method, an oil product catalyst and an oil product. The application discloses the following steps: firstly, a Na-Y zeolite raw powder and a NaOH solution are stirred and mixed to obtain a mixed solution; then, the mixed solution is cooled to room temperature; then, dilute nitric acid is used to adjust the pH value of the mixed solution cooled to room temperature, and when the pH value is adjusted to a predetermined value, the mixed solution is washed with deionized water to obtain a solid mixture; then, the solid mixture is dried to obtain a modified Y-type zeolite; and finally, the modified Y-type zeolite is uniformly mixed with a binder, an additive, a dispersant and a solvent and is stirred to obtain a uniform plastic slurry. The application adopts a NaOH desiliconization-dilute nitric acid neutralization treatment method, so that more mesopores and macropores of the zeolite molecular sieve are constructed / retained, the problem of retention and deposition of oligomerization macromolecules (C10+) is further solved, and the alkaline sites of the zeolite skeleton are not damaged.

Description

Technical Field

[0001] This invention relates to the field of petrochemical technology, and more specifically, to a method for preparing an oil catalyst, an oil catalyst, and an oil product. Background Technology

[0002] C3C4 low-carbon olefins (liquefied petroleum gas rich in propane, propylene, butane, and butene) from refineries are the main byproducts of catalytic cracking, steam cracking, and natural gas processing units, traditionally used as fuel gas or liquefied petroleum gas for civilian use. With the deepening of refinery processing and large-scale substitution with natural gas, a structural surplus of C3C4 low-carbon olefins has emerged, resulting in prices that have long been lower than naphtha. How to convert low-value C3C4 low-carbon olefins into high-value-added gasoline components and aviation kerosene that can be directly blended to meet China VI emission standards has become a common resource optimization challenge for the refining and chemical industry. In the 1960s, Gulf Oil first used a solid phosphoric acid (SPA) catalyst to oligomerize C3-C4 olefins in refinery gas into "thermal cracked gasoline," laying the foundation for the "light olefins → gasoline" concept. Subsequently, in 1982, Mobil discovered that ZSM-5 molecular sieves could simultaneously complete oligomerization-cyclization-dehydrogenation reactions to generate isomeric alkane / aromatic mixtures with octane numbers >90, marking the birth of the modern "oligomerization to gasoline" catalytic system.

[0003] There are currently two main routes for the conversion of low-carbon olefins: One method is alkylation, which uses isobutane and C3C4 olefins (such as butene) as raw materials. Under conditions of 0-180℃ and 0.3-1.0 MPa, liquid HF, concentrated H2SO4 or solid acid (USY, β zeolite, heteropoly acid / Al2O3) catalysts are used to carry out liquid-phase or gas-phase alkylation reactions. Under low-temperature and strong acid conditions, isooctane (trimethylpentane) gasoline components with RON 92-96 are obtained. Chinese patents CN1014247B and CN104393644B have described this method. Secondly, aromatization is carried out using C3C4 low-carbon olefins or liquefied petroleum gas as raw materials. Under conditions of 400-550℃, 0.1-3.0MPa, and hydrogenation or non-hydrogenation, a Zn-, Ga-, or Ni-modified ZSM-5 / HZSM-5 molecular sieve catalyst is used to carry out an oligomerization-cyclization-dehydrogenation aromatization reaction. Under the action of acid centers at higher temperatures, high-octane gasoline blending components such as benzene, toluene, xylene (BTX), and C9+ aromatics are obtained. Chinese patents CN102030605B, CN1340601A, and CN110721734A have described this process.

[0004] Compared to traditional alkylation and aromatization routes, C3C4 low-carbon olefin oligomerization technology can convert low-carbon olefin mixtures into gasoline and jet fuel components in the same fixed-bed reactor. The gasoline component, after hydrogenation saturation, can be directly hydrogenated into a high-octane stable gasoline blending component, without the need for strict isobutane-olefin ratios or subsequent aromatic blending, and it also boasts a high octane number. Compared to alkylation, oligomerization also eliminates the strong corrosion caused by liquid acids, HF, or solid acids, produces no waste acid or solid waste, and poses less environmental risk. Compared to current LPG aromatization, its advantages include a reaction temperature reduction from 400-550℃ to 120℃, eliminating the need for continuous high-temperature regeneration and coking, resulting in lower overall energy consumption and a longer catalyst cycle. The aromatic content of oligomer products can be adjusted to below 20%, retaining high octane numbers while meeting China VI emission standards for aromatics. Furthermore, hydrogen consumption is significantly lower than alkylation, and the byproduct hydrogen is superior to aromatization, thus achieving the most adaptable feedstock and the most optimal investment, environmental protection, and energy consumption-based LPG high-value-added route.

[0005] In existing technologies, CN118878390A uses a 10% Ni(CA) / S-70 boron-modified nickel-based catalyst to oligomerize propylene / n-butene into C6-C10 olefins in a fixed bed. The propylene conversion is 100%, the n-butene conversion is 78-85%, and the C8-C10 selectivity is >70%, making it suitable as a direct precursor for high-octane gasoline. However, it still requires subsequent hydrogenation saturation, and the reaction temperature is 180-220 °C, the pressure is 3-5 MPa, and the catalyst lifetime is <800 h. This method has strict requirements on the propylene / n-butene ratio and the reaction temperature is relatively high.

[0006] In the existing technology, CN202111243479B uses a mesoporous ZSM-23 molecular sieve catalyst to polymerize low-carbon olefins at 30-120℃, 1-6 MPa, and a volume hourly space velocity of 0.6-1.5 h⁻¹. It exhibits high activity and easy product separation, but the patented raw materials are limited to a mixture of C4 and C5 olefins, preferably isobutylene and isopentene, resulting in numerous reactant limitations. Furthermore, the products have a wide boiling range and low selectivity for gasoline and kerosene.

[0007] In the existing technology, CN202311416188 describes a process where propylene / butene is mixed with a diluent and then fed into a supported MWW catalyst at 60-240℃, 0.5-6 MPa, and a mass hourly space velocity of 0.5-5 h⁻¹. The single-pass conversion rate is >90%, and the oil yield is >85%. The disadvantages are that the reaction temperature range is wide, with a maximum of 240℃, and two-stage activation is required, resulting in a relatively long process.

[0008] This patent aims to develop a low-energy-consumption catalyst preparation method and process for the high-value utilization of low-carbon olefins to produce oil products, overcoming the shortcomings of existing technologies, including: (1) Compared with the aggregation route, traditional aromatization and other technologies have higher reaction temperatures and higher energy consumption; (2) Compared with oligomerization, traditional alkylation and other technologies involve strong acids, which not only corrode equipment but also generate waste acid and solid waste, resulting in significant environmental pressure. Furthermore, they have strict requirements on the ratio of alkanes to olefins in the raw materials, making them unsuitable for the harsh operating conditions in refineries where multiple low-carbon olefin components coexist. Currently, some C3C4 low-carbon olefin oligomerization catalysts suffer from problems such as excessively high reaction temperatures, strict requirements on feedstock component ratios making them difficult to adapt to demanding operating conditions where multiple components coexist, and low gasoline and kerosene yields. C10+ oligomers easily clog micropores after formation, resulting in high diffusion resistance due to insufficient mesopores / macropores, short single-pass lifespan, and the need for frequent regeneration. Existing oligomerization catalysts require further improvement. Summary of the Invention

[0009] This invention proposes a method for preparing an oil catalyst, an oil catalyst and an oil product, which can solve problems such as insufficient high-value conversion of C3C4 low-carbon olefins in refineries, high reaction temperature of traditional olefin oligomerization catalysts, difficulty in adapting to the harsh operating conditions of multiple components coexisting in C3C4 low-carbon olefins, and low gasoline and kerosene yields.

[0010] The technical solution of this invention is implemented as follows: According to a first aspect of the present invention, a method for preparing an oil catalyst is provided, comprising: The pre-prepared Na-Y zeolite powder and NaOH solution were stirred and mixed to obtain a mixed solution; the mixed solution was then cooled to room temperature. The pH of the mixed solution cooled to room temperature was adjusted using pre-prepared dilute nitric acid. Once the pH was adjusted to a predetermined value, the solution was washed with deionized water to obtain a solid mixture. The solid mixture was dried to obtain modified Y-type zeolite; The modified Y-type zeolite was mixed and stirred evenly with a pre-prepared binder, additives, dispersant and solvent to obtain a uniform plastic slurry; and the uniform plastic slurry was subjected to particle forming treatment to obtain plastic particles. The obtained plastic particles are subjected to heating and calcination activation treatment to obtain alkaline Y-type zeolite molecular sieves, which are used as oil catalysts.

[0011] Preferably, the ratio of the Na-Y zeolite powder to the NaOH solution is: 100-1000 mL of NaOH solution is added for every 10-50 g of zeolite powder; the concentration of the NaOH solution is 0.05-1 mol / L. The mixing conditions for the Na-Y zeolite powder and the NaOH solution are: stirring in a constant temperature oil bath at 70-100℃ for 2-4 hours.

[0012] Preferably, the predetermined pH value is 7-9; and the number of times the deionized water is washed is 3-5 times; the drying temperature of the solid mixture is 80-120℃, and the drying time is 12-24 h; the temperature of the heating calcination activation treatment is 450-600℃, and the time is 4-7 h.

[0013] Preferably, the binder includes one or more of boehmite, silica sol, sodium aluminate, etc., and the proportion of the binder is 15-30% of the mass of the modified Y-type zeolite.

[0014] Preferably, the additives include one or more such as guar gum powder and methylcellulose, and the proportion of the additives is 1-3% of the mass of the modified Y-type zeolite.

[0015] Preferably, the dispersant includes one or more of nitric acid, citric acid, acetic acid, and ammonia, and the proportion of the dispersant is 0.2-2% of the mass of the modified Y-type zeolite.

[0016] Preferably, the solvent includes one or more of deionized water, ethylene glycol, and water-ethanol mixture, and the proportion of the solvent is 40-70% of the mass of the modified Y-type zeolite.

[0017] According to a second aspect of the present invention, an oil catalyst is provided, wherein the oil catalyst is an oil catalyst prepared by any of the above-described oil catalyst preparation methods.

[0018] According to a third aspect of the present invention, an oil product is provided, said oil product being an oil product prepared from the above-mentioned oil product catalyst.

[0019] Preferably, the oil product includes gasoline or kerosene.

[0020] Beneficial effects: Through the implementation of this invention, a C3 / C4 olefin mixture is converted into a high-octane gasoline blending component in one step at a relatively low temperature of 120°C, with an olefin conversion rate of 95%, a gasoline yield of 75% and a kerosene yield of 25% in the liquid products. It is also applicable to the complex component conditions of low-carbon olefins in refineries, effectively promoting the high-value utilization of low-carbon olefins in refineries.

[0021] This invention employs a NaOH desilication-dilute nitric acid neutralization treatment method to construct / retain more mesopores / macropores in zeolite molecular sieves, further solving the problem of oligomeric macromolecule (C10+) retention and deposition, while preserving the alkaline sites of the zeolite framework. This promises to achieve high-value conversion of C3C4 low-carbon olefins while maintaining a longer service life.

[0022] This invention can effectively convert C3 and C4 low-carbon olefins into high-value-added gasoline and kerosene. Specifically, in an oligomerization reactor, a catalyst prepared using an oil catalyst preparation method is employed, simulating a mixture of C3 and C4 low-carbon olefins from a refinery as raw materials. The reaction is carried out at 120°C, a pressure of 6 MPa, and a mass hourly space velocity of 0.72 h⁻¹. -1 Under the specified conditions, the olefin conversion rate was approximately 95%, with gasoline yielding approximately 75% and kerosene yielding approximately 25% in the liquid products. The above conversion rates and yields were determined by gas chromatography under the following chromatographic conditions: 50 m × 0.25 mm × 0.25 μm nonpolar column, FID detector, and internal standard method for quantification. Therefore, it is evident that oligomeric molecular sieve catalysts can be used to polymerize C3C4 low-carbon olefins into gasoline and kerosene components, achieving a simpler and more valuable utilization of C3C4 low-carbon olefins. Attached Figure Description

[0023] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0024] Figure 1 This is a process flow diagram of an oil catalyst preparation method according to an embodiment of the present invention; Figure 2 This is a table of the composition of the mixed C3 feedstock; Figure 3 This is a table of the composition of mixed C4 feedstocks; Figure 4 This is a table showing the raw material composition of a mixture of mixed C3 and mixed C4 in a 1:1 ratio; Figure 5 This is a schematic diagram of the olefin conversion rate in an oligomerization reaction of a method for preparing an oil product according to an embodiment of the present invention. Figure 6 This is a flowchart of an olefin oligomerization process for a method of preparing an oil product according to an embodiment of the present invention. Figure 7 This is a schematic diagram of the yield of oligomerization reaction liquid product in an oil preparation method according to an embodiment of the present invention.

[0025] In the diagram, 1. Mixed C4 feed tank; 2. Mixed C3 feed tank; 3. Centrifugal pump; 4. Olefin oligomerization reactor; 5. Oil catalyst preparation method; 6. High-pressure separator; 7. Low-pressure separator; 8. Refrigerant; 9. Offline chromatography; 10. Online chromatography. Detailed Implementation

[0026] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention are within the scope of protection of the present invention.

[0027] Example 1 Figure 1 An embodiment of a method for preparing an oil catalyst according to the present invention is shown.

[0028] In this optional embodiment, the preparation process of the oil catalyst includes: Step S101: The pre-prepared Na-Y zeolite powder and NaOH solution are stirred and mixed to obtain a mixed solution; and the mixed solution is cooled to room temperature. Step S103: The pH value of the mixed solution cooled to room temperature is adjusted using pre-prepared dilute nitric acid. When the pH value is adjusted to a predetermined value, it is washed with deionized water to obtain a solid mixture. Step S105: The solid mixture is dried to obtain modified Y-type zeolite; Step S107: The modified Y-type zeolite is mixed and stirred evenly with the pre-prepared binder, additives, dispersant and solvent to obtain a uniform plastic slurry; and the uniform plastic slurry is subjected to particle forming treatment to obtain plastic particles. Step S109 involves heating and calcining the obtained plastic particles to activate them, thereby obtaining alkaline Y-type zeolite molecular sieves, which are used as oil catalysts.

[0029] In this optional embodiment, the ratio of the Na-Y zeolite powder to the NaOH solution is: 100-1000 mL of NaOH solution is added for every 10-50 g of zeolite powder; the concentration of the NaOH solution is 0.05-1 mol / L. The mixing conditions for the Na-Y zeolite powder and the NaOH solution are: stirring in a constant temperature oil bath at 70-100℃ for 2-4 hours.

[0030] In this optional embodiment, the predetermined pH value is 7-9; and the number of times the deionized water is washed is 3-5 times; the drying temperature of the solid mixture is 80-120℃, and the drying time is 12-24 h; the temperature of the heating calcination activation treatment is 450-600℃, and the time is 4-7 h.

[0031] In this optional embodiment, the binder includes one or more of the following: boehmite, silica sol, sodium aluminate, etc., and the proportion of the binder is 15-30% of the mass of the modified Y-type zeolite.

[0032] In this optional embodiment, the additives include one or more such as guar gum powder and methylcellulose, and the proportion of the additives is 1-3% of the mass of the modified Y-type zeolite.

[0033] In this optional embodiment, the dispersant includes one or more of nitric acid, citric acid, acetic acid, and ammonia, and the proportion of the dispersant is 0.2-2% of the mass of the modified Y-type zeolite.

[0034] In this optional embodiment, the solvent includes one or more of deionized water, ethylene glycol, and water-ethanol mixture, and the proportion of the solvent is 40%-70% of the mass of the modified Y-type zeolite.

[0035] For the above-mentioned oil catalysts, in practical applications, the finished oil catalyst can be a Y-type molecular sieve with a SiO2 / Al2O3 molar ratio of 5-7 and a total alkali content (calculated as Na2O) ≤0.5 wt% as determined by XRF.

[0036] Example 2 An oil catalyst provided according to an embodiment of the present invention is an oil catalyst prepared by the above-described oil catalyst preparation method.

[0037] Example 3 According to an embodiment of the present invention, an oil product is provided, which is an oil product prepared based on the above-described oil product catalyst. This oil product can be gasoline or kerosene. For example, gasoline or kerosene can be prepared by using the above-described oil product catalyst with a mixture of C3 and a mixture of C4.

[0038] Specifically, a mixture of C3 and C4 hydrocarbons is prepared in a 1:1 weight ratio. The prepared mixture is then combined with an oil catalyst to produce a high-value-added oil product through an oligomerization reaction. The mass hourly space velocity (WHSV) of the mixture and the oil catalyst is 0.3-0.8 h⁻¹. -1 .

[0039] In practical applications, propane and propylene can be used for mixed C3; while isobutane, n-butane, trans-2-butene, n-butene, isobutene, and cis-2-butene can be used for mixed C4; the reaction temperature for the oligomerization of the low-carbon olefins is 100-150℃, and the reaction pressure for the oligomerization of the low-carbon olefins is 5-7 MPa.

[0040] To facilitate understanding of the above technical solutions of the present invention, the following will further illustrate the above technical solutions of the present invention through several specific application examples and comparative examples.

[0041] Application Example 1 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0042] Application Example 2 In practical applications, 50 g of Na-Y zeolite powder is added to a 0.5 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0043] Application Example 3 In practical applications, 50 g of Na-Y zeolite powder is added to a 0.05 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110°C for 12 h. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0044] Application Example 4 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 600°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0045] Application Example 5 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 7. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0046] Application Example 6 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 9. Then, the solution was washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. The modified Y-type zeolite (about 55 g), 15 g of pseudoboehmite and 1 g of guar gum powder were mixed evenly, 1 mL of nitric acid and 30 mL of deionized water were added, and the mixture was stirred until a uniform plastic slurry was formed. The uniform plastic slurry was then extruded into plastic granules using a single screw extruder. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0047] Application Example 7 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110°C for 12 h.

[0048] Mix the modified Y-type zeolite (about 55 g), 15 g silica sol, and 1 g guar gum powder evenly, add 1 mL nitric acid and 30 mL deionized water, stir until a uniform plastic slurry is formed, and use a single screw extruder to extrude the uniform plastic slurry into plastic granules. The plastic particles were calcined in a muffle furnace at 550°C for 6 hours and then cooled to room temperature to obtain the finished catalyst.

[0049] Application Example 8 In practical applications, 50 g of Na-Y zeolite powder is added to a 1.0 mol / L NaOH solution, transferred to a polytetrafluoroethylene reactor, and stirred in an oil bath at 90℃ for 2 h to obtain a mixed solution. After the mixed solution was cooled to room temperature, 0.5 mol / L nitric acid solution was slowly added dropwise until the pH reached 8. The solution was then washed five times with deionized water to obtain a solid mixture. The solid mixture was then dried in an oven at 110℃ for 12 h to obtain modified Y-type zeolite. Mix the modified Y-type zeolite (about 55 g), 15 g sodium aluminate and 1 g guar gum powder evenly, add 1 mL nitric acid and 30 mL deionized water, stir until a uniform plastic slurry is formed, and use a single screw extruder to extrude the uniform plastic slurry into plastic granules. The plastic particles were placed in a muffle furnace and calcined at 550°C for 5 hours, and then cooled to room temperature to obtain the finished catalyst.

[0050] Comparative Example 1 In practical applications, 50 g of Na-Y zeolite powder, 15 g of pseudoboehmite, and 1 g of guar gum powder are mixed evenly, 1 mL of nitric acid and 30 mL of deionized water are added, and the mixture is stirred until a uniform plastic slurry is formed. The uniform plastic slurry is then extruded into plastic particles using a single-screw extruder. The plastic particles are then placed in a muffle furnace and calcined at 550°C for 5 h. After cooling to room temperature, the finished catalyst is obtained.

[0051] Comparative Example 2 In practical applications, 50 g of Na-Y zeolite powder and 1.5 g of guar gum powder are mixed evenly, 25 mL of deionized water is added, and the mixture is stirred until a uniform plastic slurry is formed. The uniform plastic slurry is then extruded into plastic particles using a single-screw extruder. The plastic particles are then placed in a muffle furnace and calcined at 550°C for 5 h. After cooling to room temperature, the finished catalyst is obtained.

[0052] By comparing the experimental groups of Application Examples 1 to 8 with the control group consisting of Comparative Examples 1 and 2, the catalytic effect of the catalyst can be obtained. That is, the catalyst prepared by the method of preparing oil catalyst uses a mixture of mixed C3 and mixed C4 components of low-carbon olefins from a simulated refinery as raw material (mixing ratio 1:1, specific composition...). Figures 2-4 Using helium as the carrier gas, the reaction was carried out at a temperature of 120°C, a pressure of 6.0 MPa, and a mass hourly space velocity of 0.72 h⁻¹. -1 Under certain conditions, a polymerization reaction experiment was conducted.

[0053] Based on the above application examples and Figures 6-7 As can be seen, the olefin conversion rate in Application Example 1 was approximately 95%, with gasoline yielding approximately 75% and kerosene yielding approximately 25% in the liquid products. This demonstrates that the separated olefins can be polymerized using an alkaline Y-type zeolite molecular sieve catalyst to produce gasoline and kerosene components, achieving a simpler and more valuable utilization of low-carbon olefins.

[0054] The above description is only a preferred embodiment of the present invention and is 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. A method for preparing an oil catalyst, characterized in that, include: The pre-prepared Na-Y zeolite powder and NaOH solution were stirred and mixed to obtain a mixed solution; The mixed solution was then cooled to room temperature. The pH of the mixed solution cooled to room temperature was adjusted using pre-prepared dilute nitric acid. Once the pH was adjusted to a predetermined value, the solution was washed with deionized water to obtain a solid mixture. The solid mixture was dried to obtain modified Y-type zeolite; The modified Y-type zeolite was mixed and stirred evenly with a pre-prepared binder, additives, dispersant and solvent to obtain a uniform plastic slurry; and the uniform plastic slurry was subjected to particle forming treatment to obtain plastic particles. The obtained plastic particles are subjected to heating and calcination activation treatment to obtain alkaline Y-type zeolite molecular sieves, which are used as oil catalysts.

2. The method for preparing an oil catalyst according to claim 1, characterized in that, The ratio of the Na-Y zeolite powder to the NaOH solution is as follows: 100-1000 mL of NaOH solution is added for every 10-50 g of zeolite powder; the concentration of the NaOH solution is 0.05-1 mol / L. The mixing conditions for the Na-Y zeolite powder and the NaOH solution are: stirring in a constant temperature oil bath at 70-100℃ for 2-4 hours.

3. The method for preparing an oil catalyst according to claim 1, characterized in that, The predetermined pH value is 7-9; and the number of times the solid mixture is washed with deionized water is 3-5 times; the drying temperature of the solid mixture is 80-120℃, and the drying time is 12-24 h; the temperature of the calcination activation treatment is 450-600℃, and the time is 4-7 h.

4. The method for preparing an oil catalyst according to claim 1, characterized in that, The binder includes one or more of boehmite, silica sol, sodium aluminate, etc., and the proportion of the binder is 15-30% of the mass of the modified Y-type zeolite.

5. The method for preparing an oil catalyst according to claim 1, characterized in that, The additives include one or more of the following: guar gum powder, methylcellulose, etc., and the proportion of the additives is 1-3% of the mass of the modified Y-type zeolite.

6. The method for preparing an oil catalyst according to claim 1, characterized in that, The dispersant includes one or more of nitric acid, citric acid, acetic acid, and ammonia, and the proportion of the dispersant is 0.2-2% of the mass of the modified Y-type zeolite.

7. The method for preparing an oil catalyst according to claim 1, characterized in that, The solvent includes one or more of deionized water, ethylene glycol, and water-ethanol mixture, and the proportion of the solvent is 40-70% of the mass of the modified Y-type zeolite.

8. An oil catalyst, characterized in that, The oil catalyst is an oil catalyst prepared by the method described in any one of claims 1-7.

9. An oil product, characterized in that, The oil is prepared based on the oil catalyst described in claim 8.

10. The oil product according to claim 9, characterized in that, The oil products include gasoline or kerosene.

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