Controllable preparation method for producing functional material with high yield while reducing olefins in gasoline, upgraded blended gasoline and functional material

Abstract

Provided in the present invention are a controllable preparation method for producing a functional material with a high yield while reducing olefins in gasoline, an upgraded blended gasoline and a functional material. The method comprises fractionating an FCC gasoline feedstock to obtain a light gasoline fraction and a heavy gasoline fraction; the light gasoline fraction and maleic anhydride undergoing a dynamic polymerization reaction so as to obtain a functional material and a filtrate mixture component; distilling the filtrate mixture component to obtain light gasoline having a low olefin content; the heavy gasoline fraction undergoing an upgrading reaction, and then blending same with the light gasoline to obtain upgraded blended gasoline having a low olefin content and a high octane number. The present invention can produce the functional material having a large molecular weight range and strong controllability while reducing olefins.

Description

Controllable preparation method of gasoline olefin reduction and enrichment functional materials and modified blending gasoline and functional materials

[0001] Cross-reference information

[0002] This application claims priority to the Chinese patent application filed with the Patent Office of China on November 30, 2023, with application number 202311630864.7 and invention name “Controllable preparation method of gasoline olefin reduction functional materials and modified blending of gasoline and functional materials”, the entire contents of which are incorporated by reference into this application. Technical Field

[0003] The present invention relates to a method for reducing olefins in gasoline and enriching functional materials, in particular to a method for converting FCC gasoline into an oil product with low olefin content and high octane number and preparing functional materials in one step, belonging to the field of petroleum refining. Background Art

[0004] To reduce environmental pollution from automobile exhaust, stricter requirements are currently being placed on gasoline for motor vehicles, requiring an olefin content of less than 15%. However, conventional light gasoline contains higher olefin content, typically 40-50%, which significantly exacerbates environmental pollution from automobile exhaust. Therefore, finding ways to efficiently utilize light gasoline and produce high-performance products from it is of vital importance.

[0005] Patent application No. CN202010599419.9 discloses a method for catalytically reducing olefins in light gasoline. This method involves gasifying the light gasoline feedstock to obtain a vapor-phase cracking feedstock. This vapor-phase cracking feedstock is then subjected to catalytic olefin cracking to obtain a cracking reaction product. The cracking reaction product is then separated to obtain a C3 or lower stream, a vapor-phase circulating feedstock, liquefied gas, and crude gasoline. Finally, the vapor-phase circulating feedstock is recycled and combined with the vapor-phase cracking feedstock for catalytic olefin cracking. This method can effectively reduce gasoline production and olefin content in gasoline, thereby increasing ethylene and propylene production.

[0006] Patent application CN202110945889.0 discloses a catalytic conversion method for deeply reducing olefins in gasoline. This method involves introducing a high-temperature catalyst into a riser reactor, sequentially contacting it with olefin-rich pre-hydrogenated catalytic light gasoline, aromatic raffinate, and preheated catalytic feedstock, vaporizing and reacting them. After separation, pre-hydrogenation treatment, and cutting, the hydrogenated catalytic heavy gasoline and pre-hydrogenated catalytic light gasoline are uniformly mixed to produce catalytic semi-finished gasoline. This catalytic conversion method is characterized by increased gasoline and propylene production, a high degree of heavy oil conversion, and reduced olefin content in the catalytic semi-finished gasoline.

[0007] In summary, existing technologies for reducing olefins in light gasoline only achieve a unilateral reduction in olefin content, or simply polymerize to produce general-purpose materials, without generating high-performance materials with higher added value and greater future demand. These technologies also fail to achieve efficient utilization of raw materials and heat. Furthermore, these technologies suffer from complex process flows and high energy consumption. Therefore, developing a method that can simultaneously reduce olefins in gasoline and produce functional materials while simultaneously increasing octane rating to meet the requirements for gasoline product quality upgrades has become an urgent challenge.

[0008] Summary of the Invention

[0009] In order to solve the above technical problems, the purpose of the present invention is to provide a controllable preparation method of a gasoline olefin-reducing functional material.

[0010] Another object of the present invention is to provide a modified blended gasoline having the characteristics of low olefin content and high octane number.

[0011] The present invention also aims to provide a functional material having the characteristics of a wide molecular weight range, strong controllability, excellent performance and a wide range of applications.

[0012] To achieve the above object, the present invention provides a controllable preparation method of a gasoline olefin-reducing and high-yield functional material, the method comprising the following steps:

[0013] S1, cutting the FCC gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction;

[0014] S2. The light gasoline fraction obtained in S1 is subjected to a dynamic polymerization reaction with maleic anhydride under the action of an initiator, an auxiliary agent, a solvent, and a gas by two-stage heating and stirring to obtain a solid-liquid system, which is then subjected to centrifugation, separation, and vacuum drying to obtain a functional material and a filtrate mixture component;

[0015] S3, distilling the filtrate mixture components obtained in S2 to obtain light gasoline with a low olefin content and heavy components, and recycling the heavy components for polymerization reaction;

[0016] S4, subjecting the heavy gasoline fraction obtained by cutting in S1 to a reforming reaction under the action of a catalyst;

[0017] S5. The heavy gasoline reformed product obtained after the reforming reaction of S4 is blended with the light gasoline with low olefin content obtained after the distillation of S3 to obtain a reformed blending gasoline with low olefin content and high octane number.

[0018] According to a specific embodiment of the present invention, preferably, the cutting temperature of the FCC gasoline is 60-150°C, more preferably 80-120°C, and further preferably 100-120°C.

[0019] According to a specific embodiment of the present invention, preferably, in step S2, the reactor used for the polymerization reaction is a slurry bed reactor.

[0020] According to a specific embodiment of the present invention, preferably, the initiator includes one or a combination of azobisisobutyronitrile (AIBN) and azobisisoheptanenitrile (ABVN), more preferably azobisisobutyronitrile (AIBN).

[0021] According to a specific embodiment of the present invention, preferably, the auxiliary agent includes one or a combination of two or more of cashew nut shell liquid, triallyl isocyanurate, and 1,2-polybutadiene, more preferably triallyl isocyanurate. The addition of the auxiliary agent facilitates the polymerization reaction and can control the molecular weight of the material to a certain extent.

[0022] According to a specific embodiment of the present invention, preferably, the solvent includes one or a combination of two or more of ethyl acetate, isoamyl acetate, isopropyl acetate, butyl acetate or n-hexane, more preferably isoamyl acetate.

[0023] According to a specific embodiment of the present invention, preferably, the gas is nitrogen and / or hydrogen.

[0024] According to a specific embodiment of the present invention, preferably, the conditions of the dynamic polymerization reaction include: in one stage of the polymerization reaction, a reaction temperature of 30-80°C, a heating rate of 1-10°C / min, a stirring rate of 0-20r / min, a reaction time of 0.5-5h, and a reaction pressure of 0.2-3.0MPa.

[0025] In the above preparation method, preferably, the reaction temperature in one stage is 40-70°C, the heating rate in one stage is 2-5°C / min, the stirring rate in one stage is 0-10 r / min, the reaction time in one stage is 1-3 h, and the reaction pressure in one stage is 0.5-1.5 MPa.

[0026] According to a specific embodiment of the present invention, preferably, the conditions of the dynamic polymerization reaction also include: in the two-stage polymerization reaction, the second-stage reaction temperature is 50-150°C, the second-stage heating / cooling rate is 1-10°C / min, the second-stage stirring rate is 10-60r / min, the second-stage reaction time is 1-6h, and the second-stage reaction pressure is 0.2-3.0MPa.

[0027] In the above preparation method, preferably, the second-stage reaction temperature is 60-100°C, the second-stage heating / cooling rate is 3-6°C / min, the second-stage stirring rate is 20-50r / min, the second-stage reaction time is 2-5h, and the second-stage reaction pressure is 0.5-1.5MPa.

[0028] The present invention carries out dynamic process control during the polymerization reaction. In the first stage of the reaction, the temperature is gradually increased and stirred. In the second stage of the reaction, stirring is added, that is, dynamic reaction, to achieve controllable polymerization preparation.

[0029] In the above preparation method, preferably, the mass ratio of light gasoline, maleic anhydride, initiator, auxiliary agent and solvent in the raw materials of the polymerization reaction is (45-152): (11-65): 1: (0.05-1): (145-389).

[0030] According to a specific embodiment of the present invention, preferably, in step S3, the distillation temperature is 25-60°C, more preferably 30-50°C.

[0031] According to a specific embodiment of the present invention, preferably, in step S4, the reactor used for the upgrading reaction is selected from a fixed bed reactor, a moving bed reactor or a fluidized bed reactor, without strict limitation.

[0032] According to a specific embodiment of the present invention, preferably, the olefin content of the FCC gasoline is greater than or equal to 30%, preferably greater than or equal to 34%, such as 34%-38%.

[0033] According to a specific embodiment of the present invention, preferably, the olefin content of the light gasoline fraction is greater than or equal to 39%, preferably greater than or equal to 43%, such as 39%-47%.

[0034] According to a specific embodiment of the present invention, preferably, the reaction temperature of the upgrading reaction is 90-380°C, more preferably 150-260°C.

[0035] According to a specific embodiment of the present invention, preferably, the reaction pressure of the upgrading reaction is 0.1-5.0 MPa, more preferably 0.5-2.5 MPa.

[0036] According to a specific embodiment of the present invention, preferably, the mass space velocity of the upgrading reaction is 0.1-5.0h -1 , more preferably 0.5-2.0h -1 .

[0037] According to a specific embodiment of the present invention, hydrogen is used as the carrier gas for the reforming reaction. Preferably, the flow rate of the reforming reaction carrier gas is 20-120 mL / min, more preferably 40-100 mL / min.

[0038] According to a specific embodiment of the present invention, preferably, the catalyst includes one or a combination of two or more of ZSM-5 molecular sieve, ZSM-11 molecular sieve, ZSM-5 / ZSM-11 eutectic molecular sieve, MCM-56 molecular sieve and β molecular sieve, more preferably ZSM-5 / ZSM-11 eutectic molecular sieve.

[0039] In the above preparation method, preferably, the silicon-aluminum molar ratio of the ZSM-5 molecular sieve is SiO2 / Al2O3=30-400, more preferably SiO2 / Al2O3=90-270.

[0040] In the above preparation method, preferably, the silicon-aluminum molar ratio of the ZSM-11 molecular sieve is SiO2 / Al2O3=30-400, more preferably SiO2 / Al2O3=120-300.

[0041] In the above preparation method, preferably, the silicon-aluminum molar ratio of the ZSM-5 / ZSM-11 eutectic molecular sieve is SiO2 / Al2O3=30-400, more preferably SiO2 / Al2O3=120-270.

[0042] In the above preparation method, preferably, the silicon-aluminum molar ratio of the MCM-56 molecular sieve is SiO2 / Al2O3=30-400, more preferably SiO2 / Al2O3=150-300.

[0043] In the above preparation method, preferably, the silicon-aluminum molar ratio of the β molecular sieve is SiO2 / Al2O3=15-300, more preferably SiO2 / Al2O3=30-150.

[0044] According to a specific embodiment of the present invention, preferably, the molding of the catalyst comprises the following steps: molding the molecular sieve catalyst with a binder, and drying and calcining the molded molecular sieve.

[0045] In the above preparation method, preferably, the binder comprises one or a combination of two or more of alumina (such as pseudo-boehmite), SB powder, silica sol and kaolin.

[0046] In the above preparation method, preferably, the drying temperature of the molecular sieve is room temperature (eg, 20°C) to 200°C, more preferably room temperature to 180°C.

[0047] In the above preparation method, preferably, the drying time of the molecular sieve is 2-24 hours, more preferably 4-24 hours.

[0048] In the above preparation method, preferably, the calcination temperature of the molecular sieve is 300-800°C, more preferably 500-600°C.

[0049] In the above preparation method, preferably, the calcination time of the molecular sieve is 2-10 h, more preferably 3-8 h.

[0050] According to a specific embodiment of the present invention, preferably, the above preparation method specifically comprises the following steps:

[0051] S1, cutting the FCC gasoline raw material through a distiller to obtain a light gasoline fraction and a heavy gasoline fraction;

[0052] S2. The light gasoline fraction obtained in S1 is introduced into a polymerization reactor to undergo polymerization reaction with maleic anhydride under the action of an initiator, an auxiliary agent, a solvent, and a gas to obtain a milky white stable solid-liquid system. The system is centrifuged, separated, and vacuum dried to obtain a white solid powder functional material and a filtrate mixture component containing unreacted light gasoline.

[0053] S3, the filtrate mixture components obtained in S2 enter the distillation tower for distillation, and the light gasoline with low olefin content is obtained at the top of the tower, and the heavy components at the bottom of the tower are recycled back to the reactor for reaction;

[0054] S4, allowing the heavy gasoline fraction with a temperature greater than 120° C. obtained by cutting in S1 to enter a reforming reactor and undergo a reforming reaction under the action of a catalyst;

[0055] S5. The heavy gasoline reformed product after the reforming reaction of S4 is blended with the light gasoline with low olefin content after distillation of S3 to obtain a reformed blending gasoline with low olefin content and high octane number.

[0056] The present invention also provides a modified blended gasoline, which is prepared by the above preparation method.

[0057] According to a specific embodiment of the present invention, preferably, the olefin content of the upgraded blended gasoline is less than 35%, preferably less than 25%, such as 3%-25%.

[0058] According to a specific embodiment of the present invention, preferably, the octane number of the upgraded blended gasoline is greater than or equal to 84, preferably greater than 90, for example 84-95.

[0059] The present invention also provides a functional material, which is prepared by the above preparation method.

[0060] According to a specific embodiment of the present invention, the molecular weight of the generated material can be controlled by controlling the reaction temperature, pressure, reaction time, and the addition of additives and initiators. Preferably, the molecular weight distribution range of the functional material is 5,000-600,000, preferably greater than 10,000, more preferably greater than 50,000, for example, 50,000-600,000.

[0061] In some specific embodiments, light gasoline undergoes polymerization and, after centrifugation, the resulting product is rich in high-performance materials. This functional material, therefore, has a wide molecular weight range and excellent performance. Depending on the molecular weight, these functional materials can be applied in various fields. Materials with a molecular weight of less than 10,000 can be used as water treatment agents and dispersants; materials with a molecular weight between 50,000 and 150,000 can be used as adhesives, pore expanders, and emulsion polymerization stabilizers; and materials with a molecular weight greater than 500,000 can be used as plastic modifiers or as stand-alone materials.

[0062] The technical solution provided by this invention converts olefins from light gasoline through polymerization and catalytic reforming reactions. This not only meets current olefin content requirements for light gasoline, but also produces urgently needed functional materials, adapting to gasoline product upgrades, product structure adjustments, and future development trends. By adjusting process parameters, the functional materials produced have a wide molecular weight range and are suitable for a wide range of applications.

[0063] The present invention has the beneficial effect of controlling the production of functional materials with varying molecular weights by dynamically polymerizing light gasoline with maleic anhydride after cutting FCC gasoline. This process also reduces the olefin content of the light gasoline. Furthermore, the octane value of heavy gasoline is increased through a reforming reaction and then blended with the distilled light gasoline with a low olefin content to produce a high-octane, low-olefin gasoline product. This achieves precise gasoline utilization, achieving gasoline quality upgrades while also enabling the controlled production of a variety of functional materials.

[0064] Compared with the existing technology, this method has the advantages of simple process flow, low energy consumption, mild reaction conditions, material circulation in the reaction process, high raw material conversion rate and product yield, precision and strong controllability. At the same time, the functional materials prepared have the characteristics of wide adjustable molecular weight range, excellent performance, strong controllability and broad application areas, providing a reference technical path for integrated refining and chemical enterprises to transform from chemical industry to new materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0065] FIG1 is a schematic flow diagram of a method for reducing olefins in gasoline and enriching functional materials provided by the present invention.

[0066] Explanation of the symbols in the accompanying drawings: 1-FCC gasoline; 2-distiller; 3-light gasoline fraction; 4-heavy gasoline fraction; 5-polymerization reactor; 6-initiator; 7-solvent; 8-gas; 9-milky white solid-liquid mixture; 10-centrifugation, separation, vacuum drying; 11-white functional material; 12-filtrate mixture components; 13-distillation tower; 14-light gasoline with low olefin content; 15-heavy components at the bottom of the tower; 16-modification reactor; 17-heavy gasoline modified product; 18-modified blending gasoline; 19-hydrogen; 20-auxiliary agent; 21-maleic anhydride. DETAILED DESCRIPTION

[0067] In order to have a clearer understanding of the technical features, objectives and beneficial effects of the present invention, the technical solution of the present invention is now described in detail below, but it should not be understood as limiting the scope of implementation of the present invention.

[0068] The representative process flow of the present invention is shown in FIG1 , which specifically includes:

[0069] FCC gasoline 1 is cut in a distiller 2 to produce a light gasoline fraction 3 and a heavy gasoline fraction 4. The light gasoline fraction 3 enters a polymerization reactor 5, where it reacts with maleic anhydride 21 under the action of an initiator 6, an auxiliary agent 20, a solvent 7, and a gas 8, undergoing a dynamic polymerization reaction through two stages of heating and stirring to produce a milky white solid-liquid mixture 9. After centrifugation, separation, and vacuum drying 10, a white functional material 11 and a filtrate mixture component 12 containing unreacted light gasoline are obtained. The filtrate mixture component 12 enters a distillation tower 13 for distillation, and a low-olefin-content light gasoline 14 is obtained at the top of the tower. The heavy component 15 at the bottom of the tower is recycled back to the polymerization reactor 5 for reaction. The cut heavy gasoline fraction 4 enters a reforming reactor 16 in a hydrogen atmosphere 19 and undergoes a reforming reaction under the action of a catalyst. The reformed heavy gasoline product 17 after the reforming reaction is blended with the low-olefin-content light gasoline 14 after distillation to produce a reformed blended gasoline 18 with a low olefin content and a high octane number.

[0070] Example 1

[0071] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0072] FCC gasoline (olefin content 35%) was cut, and a light gasoline fraction with a cutting temperature of less than 120°C was used as a raw material (olefin mass content 49%). 97.3871g of the light gasoline fraction, 14.723g of maleic anhydride, 0.4065g of an initiator (azobisisobutyronitrile), 0.1072g of an auxiliary agent (cashew nut shell oil), 245.3200g of isoamyl acetate and H2 were subjected to a dynamic polymerization reaction. In one stage of the polymerization reaction, the reaction temperature was 50°C, the heating rate was 2°C / min, and the stirring rate was 1r / min. min, a first-stage reaction time of 1 hour, and a first-stage reaction pressure of 0.5 MPa. In the second-stage polymerization reaction, the second-stage reaction temperature was 80°C, the second-stage heating rate was 3°C / min, the second-stage stirring rate was 10 r / min, the second-stage reaction time was 2 hours, and the second-stage reaction pressure was 3.0 MPa. After completion of the polymerization, a milky white solid-liquid mixture was obtained. Centrifugation, separation, and drying were performed to obtain a white functional material. The filtrate mixture was then distilled at 30°C to obtain light gasoline with a low olefin content and a heavy component, which was recycled for polymerization. The yield was calculated to be 24.0% based on the light gasoline fraction at 120°C. The molecular weight was tested to be 115,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0073] The heavy gasoline fraction with a temperature greater than 120°C obtained by cutting was used as the raw material for the reforming reaction in a fixed-bed reactor. The catalyst was loaded with ZSM-5 molecular sieve catalyst (SiO2 / Al2O3=120). The reaction temperature was 360°C, the pressure was 0.5 MPa, and the mass space velocity was 1.5 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 30 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 30°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 4% and the octane number was 92 (RON).

[0074] Example 2

[0075] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0076] FCC gasoline (olefin content 34%) was cut, and light gasoline fraction with a cutting temperature below 90°C was used as a raw material (olefin content 40%). 80.1533g of light gasoline fraction, 18.064g of maleic anhydride, 0.3187g of initiator (azobisisobutyronitrile), 0.0096g of auxiliary agent (1,2-polybutadiene) and solvent (100.2172g of isopropyl acetate and 116.2342g of butyl acetate) were subjected to dynamic polymerization reaction with H2. In one stage of polymerization reaction, the reaction temperature was 40°C, the heating rate was 2°C / min, and the reaction temperature was 100.2172g. The first stage was stirred at a rate of 5 r / min, the first stage was for a reaction time of 0.5 h, and the first stage was under a pressure of 2.0 MPa. In the second stage polymerization reaction, the second stage temperature was 60°C, the second stage heating rate was 8°C / min, the second stage stirring rate was 20 r / min, the second stage reaction time was 6 h, and the second stage pressure was 2.0 MPa. After completion of the polymerization, a milky white solid-liquid mixture was obtained. Centrifugation, separation, and drying were performed to obtain a white functional material. The filtrate mixture was then distilled at 25°C to obtain light gasoline with a low olefin content and a heavy component. The heavy component was recycled for polymerization. The yield was calculated to be 26.1% based on the light gasoline fraction at 90°C. The molecular weight was measured to be 58,000, making it suitable for use as a binder and emulsion polymerization stabilizer.

[0077] The heavy gasoline fraction with a temperature greater than 90°C obtained by cutting was used as the raw material for the reforming reaction in a fixed-bed reactor. The catalyst was loaded with ZSM-5 molecular sieve catalyst (SiO2 / Al2O3=90). The reaction temperature was 160°C, the pressure was 0.5 MPa, and the mass space velocity was 0.8 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 20 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 25°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 4% and the octane number was 88 (RON).

[0078] Example 3

[0079] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0080] FCC gasoline (olefin content 32%) was cut, and a light gasoline fraction with a cutting temperature of less than 60°C was used as a raw material (olefin mass content 39%). 92.5192g of the light gasoline fraction, 13.296g of maleic anhydride, 0.5122g of an initiator (azobisisoheptanenitrile), 0.2034g of an auxiliary agent (1,2-polybutadiene), and 189.2368g of n-hexane were used to undergo a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 60°C, the heating rate was 5°C / min, and the stirring rate was 10r. / min, the first reaction time is 1h, and the first pressure is 2.5MPa. In the second stage polymerization reaction, the second reaction temperature is 100°C, the second stage heating rate is 2°C / min, the second stage stirring rate is 30r / min, the second stage reaction time is 3h, and the second stage reaction pressure is 2.5MPa. After the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, and drying, a white functional material is obtained. The filtrate mixture is then distilled at 28°C to obtain light gasoline with a low olefin content and heavy components. The heavy components are recycled for polymerization. The yield is calculated to be 21.7% based on the light gasoline fraction at 60°C. The molecular weight is tested to be 23,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0081] The heavy gasoline fraction with a temperature greater than 60°C obtained by cutting was used as raw material for the reforming reaction in a fixed-bed reactor. The catalyst was loaded with ZSM-5 molecular sieve catalyst (SiO2 / Al2O3=150). The reaction temperature was 200°C, the pressure was 4.5MPa, and the mass space velocity was 0.6h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 50 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 28°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 12% and the octane number was 90 (RON).

[0082] Example 4

[0083] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0084] FCC gasoline (olefin content 38%) was cut, and a light gasoline fraction with a cutting temperature below 130°C was used as a raw material (olefin content 46%). 24.3890 g of the light gasoline fraction, 4.8760 g of maleic anhydride, 0.2438 g of an initiator (azobisisobutyronitrile), 0.1392 g of an auxiliary agent (triallyl isotricyanate), and a solvent (24.1933 g of isoamyl acetate and 12.3856 g of n-hexane) were subjected to dynamic polymerization with N2. In one stage of the polymerization reaction, the reaction temperature was 55°C, the heating rate was 8°C / min, and the reaction temperature was 100°C / min. The first stage was stirred at a rate of 20 r / min, the first stage was for a reaction time of 5 hours, and the first stage was under a pressure of 1.5 MPa. In the second stage polymerization reaction, the second stage temperature was 75°C, the second stage heating rate was 5°C / min, the second stage stirring rate was 50 r / min, the second stage reaction time was 5 hours, and the second stage pressure was 2.0 MPa. After completion of the polymerization, a milky white solid-liquid mixture was obtained. Centrifugation, separation, and drying were performed to obtain a white functional material. The filtrate mixture was then distilled at 32°C to obtain light gasoline with a low olefin content and a heavy component. The heavy component was recycled for polymerization. The yield was calculated to be 18.9% based on the light gasoline fraction at 130°C. The molecular weight was measured to be 159,000, making it suitable for use as a binder, pore expander, and emulsion polymerization stabilizer.

[0085] The heavy gasoline fraction with a temperature greater than 130°C obtained by cutting was used as raw material for the reforming reaction in a fixed-bed reactor. The catalyst was loaded with ZSM-5 / ZSM-11 eutectic molecular sieve catalyst (SiO2 / Al2O3=180). The reaction temperature was 300°C, the pressure was 1.5 MPa, and the mass space velocity was 2.5 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 35 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 32°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 3% and the octane number was 90 (RON).

[0086] Example 5

[0087] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0088] FCC gasoline (olefin content 34%) was cut, and a light gasoline fraction with a cutting temperature of less than 80°C was used as a raw material (olefin mass content 43%). 30.545g of the light gasoline fraction, 30.545g of maleic anhydride, 0.6109g of an initiator (azobisisobutyronitrile), 0.5254g of an auxiliary agent (1,2-polybutadiene) and 189.379g of isoamyl acetate were subjected to a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 30°C, the heating rate was 2°C / min, and the stirring rate was 2r. / min, a first-stage reaction time of 1h, and a first-stage pressure of 1.0MPa. In the second-stage polymerization reaction, the second-stage reaction temperature is 100°C, the second-stage heating rate is 4°C / min, the second-stage stirring rate is 20r / min, the second-stage reaction time is 6h, and the second-stage reaction pressure is 2.0MPa. After the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, and drying, a white functional material is obtained. The filtrate mixture is then distilled at 42°C to obtain light gasoline with a low olefin content and heavy components. The heavy components are recycled for polymerization. The yield is calculated to be 39.5% based on the light gasoline fraction at 80°C. The molecular weight is tested to be 255,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0089] The heavy gasoline fraction with a temperature greater than 80°C obtained by cutting was used as the raw material for the reforming reaction in a fixed-bed reactor. The catalyst was loaded with ZSM-5 / ZSM-11 eutectic molecular sieve catalyst (SiO2 / Al2O3=60). The reaction temperature was 220°C, the pressure was 1.2 MPa, and the mass space velocity was 1.0 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 50 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 42°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 6% and the octane number was 84 (RON).

[0090] Example 6

[0091] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0092] FCC gasoline (olefin content 33%) was cut, and a light gasoline fraction with a cutting temperature of less than 100°C was used as a raw material (olefin mass content 45%). 55.4321g of the light gasoline fraction, 21.0596g of maleic anhydride, 0.0554g of an initiator (azobisisoheptanenitrile), 0.0096g of an auxiliary agent (cashew nut shell oil), and 166.2918g of ethyl acetate were subjected to a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 50°C, the heating rate was 5°C / min, and the stirring rate was 5r / min. min, a first-stage reaction time of 4 hours, and a first-stage pressure of 2.5 MPa. In the second-stage polymerization reaction, the second-stage reaction temperature was 120°C, the second-stage heating rate was 2°C / min, the second-stage stirring rate was 30 r / min, the second-stage reaction time was 2 hours, and the second-stage reaction pressure was 2.5 MPa. After completion of the polymerization, a milky white solid-liquid mixture was obtained. After centrifugation, separation, and drying, a white functional material was obtained. The filtrate mixture was then distilled at 49°C to obtain light gasoline with a low olefin content and heavy components. The heavy components were recycled for polymerization. The yield was calculated to be 39.8% based on the light gasoline fraction at 100°C. The molecular weight was tested to be 125,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0093] The heavy gasoline fraction with a temperature greater than 100°C obtained by cutting was used as raw material for the reforming reaction in a fixed bed reactor. The catalyst ZSM-5 / ZSM-11 eutectic molecular sieve (SiO2 / Al2O3=90) was loaded and the reaction temperature was 380°C, the pressure was 3.5 MPa, and the mass space velocity was 1.5 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 60 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 49°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 6% and the octane number was 89 (RON).

[0094] Example 7

[0095] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0096] FCC gasoline (olefin content 38%) was cut, and a light gasoline fraction with a cutting temperature of less than 120°C was used as a raw material (olefin mass content 47%). 50.5364g of the light gasoline fraction, 28.4265g of maleic anhydride, 0.6317g of an initiator (azobisisoheptonitrile), 0.5427g of an auxiliary agent (triallyl isotricyanate) and 129.4985g of a solvent (isopropyl acetate) were subjected to a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 80°C, the heating rate was 10°C / min, and the stirring rate was 0. The reaction temperature was 10 r / min, the first reaction time was 5 hours, and the first pressure was 0.5 MPa. In the second stage polymerization reaction, the second reaction temperature was 110°C, the second heating rate was 3°C / min, the second stirring rate was 30 r / min, the second reaction time was 6 hours, and the second reaction pressure was 2.5 MPa. After the polymerization was completed, a milky white solid-liquid mixture was obtained. After centrifugation, separation, and drying, a white functional material was obtained. The filtrate mixture was then distilled at 37°C to obtain light gasoline with a low olefin content and heavy components. The heavy components were recycled for polymerization. The yield was calculated to be 25.3% based on the light gasoline fraction at 120°C. The molecular weight was tested to be 103,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0097] The heavy gasoline fraction with a temperature greater than 120°C obtained by cutting was used as the raw material for the reforming reaction in a fixed bed reactor. The catalyst of β molecular sieve (SiO2 / Al2O3=30) was loaded and the reaction temperature was 260°C, the pressure was 1.0 MPa, and the mass space velocity was 1.5 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 100 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 37°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 4% and the octane number was 92 (RON).

[0098] Example 8

[0099] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0100] FCC gasoline (olefin content 36%) was cut, and a light gasoline fraction with a cutting temperature of less than 140°C was used as a raw material (olefin mass content 47%). 58.7881 g of the light gasoline fraction, 24.4952 g of maleic anhydride, 0.4899 g of an initiator (azobisisobutyronitrile), 0.2450 g of an auxiliary agent (triallyl isotricyanate) and 128.3538 g of a solvent (butyl acetate) were subjected to a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 60°C, the heating rate was 3°C / min, and the stirring rate was 6. r / min, a first-stage reaction time of 0.5 h, and a first-stage pressure of 2.5 MPa. In the second-stage polymerization reaction, the second-stage reaction temperature is 120°C, the second-stage heating rate is 4°C / min, the second-stage stirring rate is 40 r / min, the second-stage reaction time is 1 h, and the second-stage reaction pressure is 2.5 MPa. After completion of the polymerization, a milky white solid-liquid mixture is obtained. After centrifugation, separation, and drying, a white functional material is obtained. The filtrate mixture is then distilled at 40°C to obtain light gasoline with a low olefin content and a heavy component. The heavy component is recycled for polymerization. The yield is calculated to be 35.8% based on the light gasoline fraction at 140°C. The molecular weight is tested to be 587,000, which can be used as a plastic modifier or a stand-alone material.

[0101] The heavy gasoline fraction with a temperature greater than 140°C obtained by cutting was used as the raw material for the reforming reaction in a fixed bed reactor. The catalyst was ZSM-11 molecular sieve (SiO2 / Al2O3=300). The reaction temperature was 320°C, the pressure was 3.0 MPa, and the mass space velocity was 2.0 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 90 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 40°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 4% and the octane number was 91 (RON).

[0102] Example 9

[0103] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0104] FCC gasoline (olefin content 37%) was cut, and a light gasoline fraction with a cutting temperature of less than 150° C. was used as a raw material (olefin mass content 44%). 50.502 g of the light gasoline fraction, 31.8960 g of maleic anhydride, 0.5316 g of an initiator (azobisisoheptanenitrile), 0.1450 g of an auxiliary agent (cashew nut shell oil), and 111.6362 g of isoamyl acetate were subjected to a dynamic polymerization reaction with H2. In one stage of the polymerization reaction, the reaction temperature was 70° C., the heating rate was 5° C. / min, and the stirring rate was 20 r / min. min, a first-stage reaction time of 3.5 hours, and a first-stage pressure of 1.5 MPa. In the second-stage polymerization reaction, the second-stage reaction temperature was 50°C, the second-stage cooling rate was 4°C / min, the second-stage stirring rate was 50 rpm, the second-stage reaction time was 2 hours, and the second-stage reaction pressure was 1.5 MPa. After completion of the polymerization, a milky white solid-liquid mixture was obtained. Centrifugation, separation, and drying were performed to obtain a white functional material. The filtrate mixture was then distilled at 31°C to obtain light gasoline with a low olefin content and a heavy component, which was recycled for polymerization. The yield was calculated to be 32.5% based on the light gasoline fraction at 150°C. The molecular weight was tested to be 287,000, making it suitable for use as a binder, pore expander, and emulsion polymerization stabilizer.

[0105] The heavy gasoline fraction with a temperature greater than 150°C obtained by cutting was used as the raw material for the reforming reaction in a fixed-bed reactor. The MCM-56 molecular sieve catalyst (SiO2 / Al2O3=150) was loaded and the reaction temperature was 340°C, the pressure was 0.8 MPa, and the mass space velocity was 2.5 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 120 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 31°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 5% and the octane number was 85 (RON).

[0106] Example 10

[0107] This embodiment provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0108] FCC gasoline (olefin content 35%) was cut, and a light gasoline fraction below the cutting temperature of 80°C was used as a raw material (olefin mass content 42%). 48.459 g of the light gasoline fraction, 10.026 g of maleic anhydride, 0.3342 g of an initiator (azobisisoheptanenitrile), 0.0985 g of an auxiliary (1,2-polybutadiene), and 93.576 g of isopropyl acetate were subjected to dynamic polymerization with N2. In one stage of the polymerization reaction, the reaction temperature was 80°C, the heating rate was 2°C / min, and the stirring rate was 5 r / min, a first-stage reaction time of 2h, and a first-stage pressure of 2.0MPa. In the second-stage polymerization reaction, the second-stage reaction temperature was 60°C, the second-stage cooling rate was 2°C / min, the second-stage stirring rate was 20r / min, the second-stage reaction time was 4h, and the second-stage reaction pressure was 2.0MPa. After the polymerization was completed, a milky white solid-liquid mixture was obtained. After centrifugation, separation, and drying, a white functional material was obtained. The filtrate mixture was then distilled at 46°C to obtain light gasoline with a low olefin content and heavy components. The heavy components were recycled for polymerization. The yield was calculated to be 23.5% based on the light gasoline fraction at 80°C. The molecular weight was tested to be 15,000, and it can be used as a binder, pore expander, and emulsion polymerization stabilizer.

[0109] The heavy gasoline fraction with a temperature greater than 80°C obtained by cutting was used as raw material for the reforming reaction in a fixed-bed reactor. The ZSM-5 molecular sieve catalyst (SiO2 / Al2O3=360) was loaded and the reaction temperature was 240°C, the pressure was 1.0 MPa, and the mass space velocity was 4.0 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 85 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 46°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 5% and the octane number was 90 (RON).

[0110] Comparative Example 1

[0111] This comparative example provides a method for reducing olefin-rich materials in gasoline, which comprises the following steps:

[0112] FCC gasoline (olefin content 20%) was cut, and a light gasoline fraction less than the cutting temperature of 50°C was used as a raw material (olefin mass content 28%). At a polymerization temperature of 50°C and a pressure of 0MPa (N2), the raw material ratio was the same as in Example 4 except that no additives (cashew nut shell oil, triallyl isocyanurate and 1,2-polybutadiene) were added. The polymerization reaction took place for 12 hours, resulting in a creamy yellow solid. No white functional material was obtained. Then, the filtrate mixture components were distilled at 60°C to obtain a light gasoline with a low olefin content and a heavy component, which was recycled for polymerization. Based on the light gasoline fraction at 50°C, the yield was calculated to be 11.1%, and its molecular weight was tested to be 2300. The heavy gasoline reformed product was blended with the light gasoline with a low olefin content after distillation at 60°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that its olefin content was 6% and its octane number was 80 (RON).

[0113] Comparative Example 2

[0114] This comparative example provides a method for reducing olefin-rich materials in gasoline, which comprises the following steps:

[0115] Using the full-fraction FCC gasoline as the raw material, without cutting, a one-stage polymerization reaction was conducted at a temperature of 100°C and a pressure of 0.5 MPa (H2). Other reaction conditions were the same as in Example 9. After the polymerization reaction, a creamy yellow solid was obtained. The yield was calculated to be 12.5% ​​based on the full-fraction FCC light gasoline raw material, and the molecular weight was measured to be 1503. After a reforming reaction using the full-fraction FCC gasoline, an olefin content of 32% and an octane number (RON) of 84 were obtained.

[0116] Comparative Example 3

[0117] This comparative example provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0118] FCC gasoline (35% olefin content) was cut and a light gasoline fraction (42% olefin content by weight) below the cut temperature of 90°C was used as the feedstock. At a polymerization temperature of 200°C and a pressure of 2.0 MPa (H₂), 53.4762g of the light gasoline fraction, 30.8325g of maleic anhydride, 0.5187g of an initiator (azobisisocyanurate), 0.1239g of an auxiliary (triallyl isocyanurate), and 102.9815g of a solvent (isoamyl acetate) were polymerized for 12 hours to produce a milky white solid-liquid mixture. Centrifugation, separation, and drying yielded a white functional material. The filtrate mixture was then distilled at 65°C to yield a low-olefin light gasoline fraction and a heavy component, which was then recycled for polymerization. The yield, calculated based on the 90°C light gasoline fraction, was 20.4%, and the molecular weight was 1286.

[0119] The heavy gasoline fraction with a temperature greater than 90°C obtained by cutting was used as raw material for the reforming reaction in a fixed bed reactor. The ZSM-5 molecular sieve catalyst (SiO2 / Al2O3=90) was loaded and the reaction temperature was 200°C, the pressure was 2.5MPa, and the hydrogen mass space velocity was 5h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 60 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 65°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 35% and the octane number was 76 (RON).

[0120] Comparative Example 4

[0121] This comparative example provides a method for reducing olefins in gasoline and enriching functional materials, which comprises the following steps:

[0122] FCC gasoline (37% olefin content) was cut and a light gasoline fraction (44% olefin content by mass) below the cut temperature of 150°C was used as the feedstock. At a polymerization temperature of 120°C and a pressure of 0.5 MPa (H₂), 16.9480g of the light gasoline fraction, 30.5064g of maleic anhydride, 0.4327g of initiator (azobisisoheptanenitrile), 0.6356g of auxiliary agent (cashew nut shell liquid), and 43.2174g of solvent (isoamyl acetate) were polymerized for 10 hours to produce a milky white solid-liquid mixture. Centrifugation, separation, and drying yielded a white functional material. The filtrate mixture was then distilled at 20°C to yield a low-olefin light gasoline fraction and a heavy component, which was then recycled for polymerization. The yield, calculated based on the 150°C light gasoline fraction, was 40.2%, and the molecular weight was 3009.

[0123] The heavy gasoline fraction with a temperature greater than 150°C obtained by cutting was used as the raw material. The reaction was carried out in a fixed bed reactor loaded with ZSM-5 / ZSM-11 molecular sieve catalyst (SiO2 / Al2O3=60). The reaction temperature was 460°C, the pressure was 0.3 MPa, and the mass space velocity was 0.3 h -1 The reforming reaction took place under the condition of a hydrogen flow rate of 80 mL / min. The heavy gasoline reformed product after the reforming reaction was blended with light gasoline with a low olefin content after distillation at 20°C to obtain a blended gasoline product with a low olefin content and a high octane number. Analysis showed that the olefin content was 14% and the octane number was 78 (RON).

[0124] As can be seen from the results of Examples 1-10 and Comparative Examples 1-4, the present invention first selects an appropriate temperature to cut gasoline into light gasoline and heavy gasoline. For the light gasoline, a dynamic polymerization method is adopted to precisely control the polymerization reaction through two different process technologies to achieve controllable preparation of functional materials with different molecular weights, thereby obtaining functional materials for different purposes. Unreacted materials are simultaneously recycled during the reaction process to improve the polymerization reaction efficiency. The heavy gasoline undergoes a modification reaction under the action of the catalyst, and through reactions such as isomerization, alkylation, and hydrogen transfer, a high-quality gasoline blending component with a high octane number and low olefin content is obtained.

Claims

1. A controllable preparation method for producing functional materials with reduced olefins from gasoline, wherein, the method comprises the following steps: S1. Cut the FCC gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction; S2. Subject the light gasoline fraction obtained in S1 to a dynamic polymerization reaction with maleic anhydride under the action of an initiator, an auxiliary agent, a solvent and a gas through two-stage temperature rise and stirring, to obtain a solid-liquid system, and after centrifugation, separation and vacuum drying, obtain a functional material and a filtrate mixture component; S3. Distill the filtrate mixture component obtained in S2 to obtain light gasoline with a low olefin content and a heavy component, and recycle the heavy component for the polymerization reaction; S4. Subject the heavy gasoline fraction obtained by cutting in S1 to a reforming reaction under the action of a catalyst; S5. Blend the heavy gasoline reformed product obtained after the reforming reaction in S4 with the light gasoline with a low olefin content obtained after distillation in S3 to obtain a reformed blended gasoline with a low olefin content and a high octane number; wherein, the cutting temperature of the FCC gasoline is 60 - 150 °C; in the polymerization reaction, the mass ratio of the light gasoline fraction, maleic anhydride, initiator, auxiliary agent, and solvent is (45 - 152):(11 - 65):1:(0.05 - 1):(145 - 389).

2. The preparation method according to claim 1, wherein, in step S2, the reactor used for the polymerization reaction is a slurry bed reactor.

3. The preparation method according to claim 1, wherein, the initiator includes one or a combination of two of azobisisobutyronitrile and azobisisoheptonitrile.

4. The preparation method according to claim 1, wherein, the auxiliary agent includes one or a combination of two or more of cashew shell oil, triallyl isocyanurate, and 1,2-polybutadiene.

5. The preparation method according to claim 1, wherein, the solvent includes one or a combination of two or more of ethyl acetate, isopentyl acetate, isopropyl acetate, butyl acetate, and n-hexane.

6. The preparation method according to claim 1, wherein, the gas is nitrogen and / or hydrogen.

7. The preparation method according to claim 1, wherein, the conditions of the dynamic polymerization reaction include: in the first-stage polymerization reaction, the first-stage reaction temperature is 30 - 80 °C, the first-stage temperature rise rate is 1 - 10 °C / min, the first-stage stirring rate is 0 - 20 r / min, the first-stage reaction time is 0.5 - 5 h, and the first-stage reaction pressure is 0.2 - 3.0 MPa.

8. The preparation method according to claim 1, wherein, the conditions of the dynamic polymerization reaction further include: in the second-stage polymerization reaction, the second-stage reaction temperature is 50 - 150 °C, the second-stage heating / cooling rate is 1 - 10 °C / min, the second-stage stirring rate is 10 - 60 r / min, the second-stage reaction time is 1 - 6 h, and the second-stage reaction pressure is 0.2 - 3.0 MPa.

9. The preparation method according to claim 1, wherein, the olefin content of the FCC gasoline is greater than or equal to 30%.

10. The preparation method according to claim 1, wherein, the olefin content of the light gasoline fraction is greater than or equal to 39%.

11. The preparation method according to claim 1, wherein, The conditions for the reforming reaction are as follows: reaction temperature is 90 - 380 °C, reaction pressure is 0.1 - 5.0 MPa, and mass space velocity is 0.1 - 5.0 h -1 .

12. The preparation method according to claim 1, wherein, the catalyst comprises one or a combination of two or more of ZSM-5 molecular sieve, ZSM-11 molecular sieve, ZSM-5 / ZSM-11 eutectic molecular sieve, MCM-56 molecular sieve, and β molecular sieve.

13. The preparation method according to claim 12, wherein, The silica-alumina molar ratio of the ZSM-5 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400.

14. The preparation method according to claim 12, wherein, The silica-alumina molar ratio of the ZSM-11 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400.

15. The preparation method according to claim 12, wherein, The silica-alumina molar ratio of the ZSM-5 / ZSM-11 eutectic zeolite is SiO 2 / Al 2 O 3 = 30 - 400.

16. The preparation method according to claim 12, wherein, The silicon-aluminum molar ratio of the MCM-56 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400.

17. The preparation method according to claim 12, wherein, The silica-alumina molar ratio of the β zeolite is SiO 2 / Al 2 O 3 = 15 - 300.

18. The preparation method according to claim 1, wherein, in step S3, the temperature of the distillation is 25 - 60 °C.

19. A reformulated blending gasoline, which is prepared by the preparation method according to any one of claims 1 - 18.

20. The reformulated blending gasoline according to claim 19, wherein, the olefin content of the reformulated blending gasoline is less than 35%.

21. The reformulated blending gasoline according to claim 19, wherein, the octane number of the reformulated blending gasoline is greater than or equal to 84.

22. A functional material, which is prepared by the preparation method according to any one of claims 1 - 18.

23. The functional material according to claim 22, wherein, the molecular weight distribution range of the functional material is 5,000 - 600,000.

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