Controllable preparation method of gasoline olefin-reducing rich-production functional material, modified blended gasoline and functional material

Abstract

The invention provides a controllable preparation method of a gasoline olefin-reducing rich-production functional material, modified blended gasoline and a functional material. The method comprises the following steps: cutting an FCC gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction; carrying out two-stage heating and stirring on the light gasoline fraction and maleic anhydride under the action of an initiator, an auxiliary agent, a solvent and gas to generate a dynamic polymerization reaction, and carrying out centrifugation, separation and vacuum drying to obtain a functional material and a filtrate mixture component; distilling the filtrate mixture components to obtain light gasoline with low olefin content and heavy components, and circularly carrying out polymerization reaction on the heavy components; carrying out modification reaction on the cut heavy gasoline fraction under the action of a catalyst; and blending the heavy gasoline modified product with light gasoline with low olefin content to obtain the modified blended gasoline with low olefin content and high octane number. The functional material prepared during olefin reduction has the characteristics of wide molecular weight range, high controllability and wide application field.

Description

Technical Field

[0001] The present invention relates to a method for reducing olefins in gasoline and enriching functional materials, and particularly to a method for converting FCC gasoline into oil products with low olefin content and high octane number, and simultaneously preparing functional materials in one step, belonging to the field of petroleum refining. Background Art

[0002] In order to reduce the environmental pollution caused by automobile exhaust, more stringent requirements are currently imposed on vehicle gasoline, and the olefin content in gasoline is required to be less than 15%. However, the olefin content in conventional light gasoline is relatively high, usually 40 - 50%, which will seriously aggravate the environmental pollution caused by automobile exhaust. Therefore, how to efficiently utilize light gasoline and obtain high-performance products from light gasoline is extremely urgent.

[0003] Patent application No. CN202010599419.9 discloses a method for reducing olefins in catalytic light gasoline. In this method, the light gasoline raw material is gasified to obtain a gas-phase cracking raw material; then the gas-phase cracking raw material is subjected to olefin catalytic cracking treatment to obtain a cracking reaction product; thereafter, the cracking reaction product is separated to obtain a C3 and lower stream, a gas-phase recycle material, liquefied gas and crude gasoline; finally, the gas-phase recycle material is recycled and merged with the gas-phase cracking raw material for olefin catalytic cracking treatment. This method can effectively reduce the gasoline production and the olefin content in gasoline, and can increase the production of ethylene and propylene.

[0004] Patent application No. CN202110945889.0 discloses a catalytic conversion method for deeply reducing gasoline olefins. In this method, a high-temperature catalyst is input into a riser reactor and successively contacts, vaporizes and reacts with pre-hydrotreated catalytic light gasoline rich in olefins, aromatics raffinate, and preheated catalytic raw materials. After separation, pre-hydrotreatment, and cutting, the hydrocatalytic heavy gasoline is mixed evenly with the pre-hydrotreated catalytic light gasoline to obtain a catalytic semi-finished gasoline. This catalytic conversion method has the characteristics of increasing gasoline production, increasing propylene production, high conversion degree of heavy oil, and reducing the olefin content of the catalytic semi-finished gasoline.

[0005] In summary, in the existing light gasoline olefin reduction technologies, only the olefin content in gasoline is unidirectionally reduced, or only general-purpose materials are polymerized, without generating high-performance materials with higher added value and greater future demand, and the efficient utilization of raw materials and heat cannot be achieved. At the same time, these technologies also have problems such as complex process flow and high energy consumption. Therefore, developing a method that can enrich functional materials while reducing olefins in gasoline and simultaneously increase the octane number to meet the requirements of gasoline product quality upgrade has become an urgent problem to be solved currently. Summary of the Invention

[0006] To solve the above technical problems, the object of the present invention is to provide a controllable preparation method for reducing olefins in gasoline and enriching functional materials.

[0007] Another object of the present invention is to provide a reformulated blending gasoline, which has the characteristics of low olefin content and high octane number.

[0008] Another object of the present invention is to provide a functional material, which has the characteristics of a wide molecular weight range, strong controllability, excellent performance, and a wide range of application fields.

[0009] To achieve the above object, the present invention provides a controllable preparation method for reducing olefins in gasoline and enriching functional materials, which method comprises the following steps:

[0010] S1. Cut the FCC gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction;

[0011] S2. Make the light gasoline fraction obtained in S1 undergo 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;

[0012] S3. Distill the filtrate mixture component obtained in S2 to obtain light gasoline with low olefin content and a heavy component, and the heavy component is recycled for the polymerization reaction;

[0013] S4. Make the heavy gasoline fraction obtained by cutting in S1 undergo a reforming reaction under the action of a catalyst;

[0014] S5. Blend the heavy gasoline reformed product obtained after the reforming reaction in S4 with the light gasoline with low olefin content obtained after distillation in S3 to obtain a reformulated blending gasoline with low olefin content and high octane number.

[0015] 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.

[0016] 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.

[0017] According to a specific embodiment of the present invention, preferably, the initiator includes one or a combination of two of azobisisobutyronitrile (AIBN) and azobisisoheptonitrile (ABVN), and more preferably azobisisobutyronitrile (AIBN).

[0018] According to the specific embodiments of the present invention, preferably, the auxiliary agent includes one or a combination of two or more of cashew shell oil, triallyl isocyanurate, and 1,2-polybutadiene, and more preferably triallyl isocyanurate. Adding the auxiliary agent is beneficial to the occurrence of the polymerization reaction and can control the molecular weight of the material to a certain extent.

[0019] According to the specific embodiments 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, and more preferably isoamyl acetate.

[0020] According to the specific embodiments of the present invention, preferably, the gas is nitrogen and / or hydrogen.

[0021] According to the specific embodiments of the present invention, preferably, the conditions for the dynamic polymerization reaction include: in the first-stage polymerization reaction, the first-stage reaction temperature is 30-80 °C, the first-stage heating 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.

[0022] In the above preparation method, preferably, the first-stage reaction temperature is 40-70 °C, the first-stage heating rate is 2-5 °C / min, the first-stage stirring rate is 0-10 r / min, the first-stage reaction time is 1-3 h, and the first-stage reaction pressure is 0.5-1.5 MPa.

[0023] According to the specific embodiments of the present invention, preferably, the conditions for 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.

[0024] 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 20-50 r / min, the second-stage reaction time is 2-5 h, and the second-stage reaction pressure is 0.5-1.5 MPa.

[0025] In the polymerization reaction process of the present invention, dynamic process control is carried out. In the first stage of the reaction, gradual heating and stirring are adopted, and stirring is increased in the second stage of the reaction, that is, dynamic reaction, to achieve controllable polymerization preparation.

[0026] 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).

[0027] According to a specific embodiment of the present invention, preferably, in step S3, the temperature of the distillation is 25-60 °C, more preferably 30-50 °C.

[0028] According to a specific embodiment of the present invention, preferably, in step S4, the reactor used for the reforming reaction is selected from a fixed bed reactor, a moving bed reactor or a fluidized bed reactor, without strict limitation.

[0029] 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%.

[0030] 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%.

[0031] According to a specific embodiment of the present invention, preferably, the reaction temperature of the reforming reaction is 90-380 °C, more preferably 150-260 °C.

[0032] According to a specific embodiment of the present invention, preferably, the reaction pressure of the reforming reaction is 0.1-5.0 MPa, more preferably 0.5-2.5 MPa.

[0033] According to a specific embodiment of the present invention, preferably, the mass space velocity of the reforming reaction is 0.1-5.0 h -1 , more preferably 0.5-2.0 h -1 .

[0034] 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 carrier gas for the reforming reaction is 20-120 mL / min, more preferably 40-100 mL / min.

[0035] 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.

[0036] In the above preparation method, preferably, the silica-aluminum molar ratio of the ZSM-5 molecular sieve is SiO 2 / Al 2 O 3 = 30-400, more preferably SiO 2 / Al 2 O 3 = 90-270.

[0037] In the above preparation method, preferably, the silica-alumina molar ratio of the ZSM-11 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 120 - 300.

[0038] In the above preparation method, preferably, the silica-alumina molar ratio of the ZSM-5 / ZSM-11 eutectic molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 120 - 270.

[0039] In the above preparation method, preferably, the silica-alumina molar ratio of the MCM-56 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 150 - 300.

[0040] In the above preparation method, preferably, the silica-alumina molar ratio of the β molecular sieve is SiO 2 / Al 2 O 3 = 15 - 300, more preferably SiO 2 / Al 2 O 3 = 30 - 150.

[0041] According to the specific embodiments of the present invention, preferably, the shaping of the catalyst includes the following steps: shaping the molecular sieve catalyst with a binder, and drying and calcining the shaped molecular sieve.

[0042] In the above preparation method, preferably, the binder includes one or a combination of two or more of alumina (such as pseudo-boehmite), SB powder, silica sol, and kaolin.

[0043] In the above preparation method, preferably, the drying temperature of the molecular sieve is from room temperature (such as 20 °C) to 200 °C, more preferably from room temperature to 180 °C.

[0044] In the above preparation method, preferably, the drying time of the molecular sieve is 2 - 24 h, more preferably 4 - 24 h.

[0045] In the above preparation method, preferably, the calcination temperature of the molecular sieve is 300 - 800 °C, more preferably 500 - 600 °C.

[0046] In the above preparation method, preferably, the calcination time of the molecular sieve is 2 - 10 h, more preferably 3 - 8 h.

[0047] According to a specific embodiment of the present invention, preferably, the above preparation method specifically comprises the following steps:

[0048] S1. Cut the FCC gasoline raw material through a distiller to obtain a light gasoline fraction and a heavy gasoline fraction;

[0049] S2. Feed the light gasoline fraction obtained in S1 into a polymerization reactor, and carry out a polymerization reaction with maleic anhydride under the action of an initiator, an auxiliary agent, a solvent and a gas to obtain a stable milky solid-liquid system. After centrifugation, separation and vacuum drying, a white solid powder functional material and a filtrate mixture component containing unreacted light gasoline are obtained;

[0050] S3. Feed the filtrate mixture component obtained in S2 into a distillation column for distillation. Light gasoline with a low olefin content is obtained at the top of the column, and the bottom heavy components are recycled to the reactor for reaction;

[0051] S4. Feed the heavy gasoline fraction greater than 120 °C obtained by cutting in S1 into a reforming reactor and carry out a reforming reaction under the action of a catalyst;

[0052] S5. Blend the heavy gasoline reformed product after the reforming reaction in S4 with the light gasoline with a low olefin content after distillation in S3 to obtain a reformed blended gasoline with a low olefin content and a high octane number.

[0053] The present invention also provides a reformed blended gasoline which is prepared by the above preparation method.

[0054] According to a specific embodiment of the present invention, preferably, the olefin content of the reformed blended gasoline is less than 35%, preferably less than 25%, such as 3% - 25%.

[0055] According to a specific embodiment of the present invention, preferably, the octane number of the reformed blended gasoline is greater than or equal to 84, preferably greater than 90, such as 84 - 95.

[0056] The present invention also provides a functional material which is prepared by the above preparation method.

[0057] According to specific embodiments of the present invention, the molecular weight of the resulting material can be controlled by controlling reaction temperature, pressure, reaction time, and conditions such as additives and initiators added. 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, such as 50,000 - 600,000.

[0058] In some specific embodiments, light gasoline undergoes a polymerization reaction. After centrifugal separation, the resulting product is rich in high-performance materials, that is, the prepared functional material has a wide molecular weight range and excellent performance. According to the molecular weight, the functional material can be applied to different fields. Those with a molecular weight less than 10,000 can be used as water treatment agents and dispersants, etc.; those with a medium molecular weight of 50,000 - 150,000 can be used as binders, pore expanders, and emulsion polymerization stabilizers; the functional material with a molecular weight greater than 500,000 can be used as a plastic modifier or used as an independent material.

[0059] The technical solution provided by the present invention converts olefins in light gasoline through polymerization and catalytic upgrading reactions. On the one hand, it meets the current requirements for olefin content in light gasoline, and on the other hand, it prepares the much-needed functional materials in the future, adapting to the upgrading of gasoline quality, the adjustment of product structure, and future development trends. By adjusting process parameters, the prepared functional material has a wide molecular weight range and has a wide range of uses.

[0060] The beneficial effects of the present invention are as follows: In the method provided by the present invention, after FCC gasoline is cut, through the dynamic polymerization reaction of light gasoline and maleic anhydride, functional materials with different molecular weights are controllably prepared, while reducing the olefin content of light gasoline. On the other hand, heavy gasoline improves the octane number through a reforming reaction and is blended with light gasoline with a low olefin content after distillation to obtain a gasoline product with a high octane number and a low olefin content, achieving the precise utilization of gasoline, meeting the upgrading of gasoline quality, and controllably preparing a variety of functional materials at the same time.

[0061] Compared with the prior art, this method has the advantages of a simple process flow, low energy consumption, mild reaction conditions, material recycling in the reaction process, high raw material conversion rate and product yield, strong precision and controllability. At the same time, the prepared functional material has the characteristics of a wide adjustable range of molecular weight, excellent performance, strong controllability, and a wide application field, providing a technical path that can be used for reference for the transformation of refining and chemical integrated enterprises from chemicals to new materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0062] Figure 1 It is a process schematic diagram of the method for reducing olefins in gasoline and enriching functional materials provided by the present invention.

[0063] Description of the reference signs in the drawings:

[0064] 1-FCC gasoline, 2-distiller, 3-light gasoline fraction, 4-heavy gasoline fraction, 5-polymerization reactor, 6-initiator, 7-solvent, 8-gas, 9-maleic anhydride, 10-milky white solid-liquid mixture, 11-white functional material, 12-filtered liquid mixture component, 13-distillation column, 14-light gasoline with low olefin content, 15-bottom heavy components, 16-reforming reactor, 17-heavy gasoline reforming product, 18-reformed and blended gasoline, 19-hydrogen, 20-additive. Detailed implementation mode

[0065] For a clearer understanding of the technical features, objectives, and beneficial effects of the present invention, the technical solution of the present invention will now be described in detail below, but it should not be construed as a limitation on the scope of implementation of the present invention.

[0066] The representative process flow of the present invention is as Figure 1 shown, specifically including:

[0067] The FCC gasoline 1 is cut by the distiller 2 to obtain a light gasoline fraction 3 and a heavy gasoline fraction 4; the light gasoline fraction 3 enters the polymerization reactor 5, and under the action of the initiator 6, additive 20, solvent 7, and gas 8, it undergoes a dynamic polymerization reaction with maleic anhydride 9 through two-stage heating and stirring to obtain a milky white solid-liquid mixture 10, which is centrifuged, separated, and vacuum dried to obtain a white functional material 11 and a filtered liquid mixture component 12 containing unreacted light gasoline; the filtered liquid mixture component 12 enters the distillation column 13 for distillation, and the distilled light gasoline 14 with low olefin content is obtained at the top of the column, and the bottom heavy components 15 are recycled to the polymerization reactor 5 for reaction; the cut heavy gasoline fraction 4 enters the reforming reactor 16 under the atmosphere of hydrogen 19 and undergoes a reforming reaction under the action of a catalyst; the heavy gasoline reforming product 17 after the reforming reaction is blended with the distilled light gasoline 14 with low olefin content to obtain a reformed and blended gasoline 18 with low olefin content and high octane number.

[0068] Example 1

[0069] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0070] The FCC gasoline (olefin content 35%) is cut, and the light gasoline fraction with a cutting temperature less than 120°C is used as the raw material (olefin mass content 49%). The light gasoline fraction is 97.3871 g, maleic anhydride is 14.723 g, initiator (azobisisobutyronitrile) is 0.4065 g, additive (cashew shell oil) is 0.1072 g, solvent (isopentyl acetate 245.3200 g), and H 2A dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 50 °C, the heating rate in the first stage is 2 °C / min, the stirring rate in the first stage is 1 r / min, the reaction time in the first stage is 1 h, and the reaction pressure in the first stage is 0.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 80 °C, the heating rate in the second stage is 3 °C / min, the stirring rate in the second stage is 10 r / min, the reaction time in the second stage is 2 h, and the reaction pressure in the second stage is 3.0 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 30 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 120 °C, its yield is calculated to be 24.0%, and its molecular weight is tested to be 115,000, which can be used as a binder, pore-expanding agent and emulsion polymerization stabilizer.

[0071] Using the heavy gasoline fraction with a cut temperature greater than 120 °C as the raw material, a reforming reaction is carried out on a fixed-bed reactor. The catalyst is filled with ZSM-5 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 120). The reforming reaction occurs under the conditions of a reaction temperature of 360 °C, a pressure of 0.5 MPa, a mass space velocity of 1.5 h -1 , and a hydrogen flow rate of 30 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 4% and the octane number is 92 (RON).

[0072] Example 2

[0073] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0074] Cut the FCC gasoline (olefin content 34%). Using the light gasoline fraction with a cut temperature less than 90 °C as the raw material (olefin mass content 40%), 80.1533 g of light gasoline fraction, 18.064 g of maleic anhydride, 0.3187 g of initiator (azobisisobutyronitrile), 0.0096 g of auxiliary agent (1,2-polybutadiene) and solvent (100.2172 g of isopropyl acetate and 116.2342 g of butyl acetate) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 40 °C, the heating rate in the first stage is 2 °C / min, the stirring rate in the first stage is 5 r / min, the reaction time in the first stage is 0.5 h, and the pressure in the first stage is 2.0 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 60 °C, the heating rate in the second stage is 8 °C / min, the stirring rate in the second stage is 20 r / min, the reaction time in the second stage is 6 h, and the reaction pressure in the second stage is 2.0 MPa; after polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 25 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for polymerization reaction. Based on the light gasoline fraction at 90 °C, its yield is calculated to be 26.1%, and its molecular weight is tested to be 58,000, which can be used as a binder and an emulsifying polymerization stabilizer.

[0075] Using the heavy gasoline fraction greater than 90 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor. The catalyst is loaded with ZSM-5 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 90). The reforming reaction occurs under the conditions of a reaction temperature of 160 °C, a pressure of 0.5 MPa, a mass space velocity of 0.8 h -1 , and a hydrogen flow rate of 20 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 4% and the octane number is 88 (RON).

[0076] Example 3

[0077] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0078] Cut the FCC gasoline (olefin content 32%), and use the light gasoline fraction less than the cutting temperature of 60 °C as the raw material (olefin mass content 39%). The light gasoline fraction is 92.5192 g, maleic anhydride is 13.296 g, initiator (azodiisooctanenitrile) is 0.5122 g, auxiliary agent (1,2-polybutadiene) is 0.2034 g, solvent (n-hexane 189.2368 g) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 60 °C, the heating rate in the first stage is 5 °C / min, the stirring rate in the first stage is 10 r / min, the reaction time in the first stage is 1 h, and the pressure in the first stage is 2.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 100 °C, the heating rate in the second stage is 2 °C / min, the stirring rate in the second stage is 30 r / min, the reaction time in the second stage is 3 h, and the reaction pressure in the second stage is 2.5 MPa; after polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 28 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for polymerization reaction. Based on the light gasoline fraction at 60 °C, its yield is calculated to be 21.7%, and its molecular weight is tested to be 23,000, which can be used as a binder, pore-expanding agent and emulsion polymerization stabilizer.

[0079] Using the heavy gasoline fraction greater than 60 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor. The catalyst is loaded with ZSM-5 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 150). The reforming reaction occurs under the conditions of a reaction temperature of 200 °C, a pressure of 4.5 MPa, a mass space velocity of 0.6 h -1 , and a hydrogen flow rate of 50 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 12% and the octane number is 90 (RON).

[0080] Example 4

[0081] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0082] Cut the FCC gasoline (olefin content 38%). Using the light gasoline fraction with a cutting temperature less than 130 °C as the raw material (olefin mass content 46%), 24.3890 g of light gasoline fraction, 4.8760 g of maleic anhydride, 0.2438 g of initiator (azobisisobutyronitrile), 0.1392 g of auxiliary agent (triallyl isocyanurate) and solvent (24.1933 g of isoamyl acetate and 12.3856 g of n-hexane) and N 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 55 °C, the heating rate in the first stage is 8 °C / min, the stirring rate in the first stage is 20 r / min, the reaction time in the first stage is 5 h, and the pressure in the first stage is 1.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 75 °C, the heating rate in the second stage is 5 °C / min, the stirring rate in the second stage is 50 r / min, the reaction time in the second stage is 5 h, and the reaction pressure in the second stage is 2.0 MPa; after polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 32 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for polymerization reaction. Based on the light gasoline fraction at 130 °C, its yield is calculated to be 18.9%, and its molecular weight is tested to be 159,000, which can be used as a binder, pore-expanding agent and emulsion polymerization stabilizer.

[0083] Using the heavy gasoline fraction greater than 130 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor. The catalyst is loaded with a ZSM-5 / ZSM-11 eutectic molecular sieve catalyst (SiO 2 / Al 2 O 3 = 180). The reforming reaction occurs under the conditions of a reaction temperature of 300 °C, a pressure of 1.5 MPa, a mass space velocity of 2.5 h -1 , and a hydrogen flow rate of 35 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 3% and the octane number is 90 (RON).

[0084] Example 5

[0085] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0086] Cut the FCC gasoline (olefin content 34%). Using the light gasoline fraction less than the cutting temperature of 80 °C as the raw material (olefin mass content 43%), 30.545 g of light gasoline fraction, 30.545 g of maleic anhydride, 0.6109 g of initiator (azobisisobutyronitrile), 0.5254 g of auxiliary agent (1,2-polybutadiene) and 189.379 g of solvent (isopentyl acetate) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 30 °C, the heating rate in the first stage is 2 °C / min, the stirring rate in the first stage is 2 r / min, the reaction time in the first stage is 1 h, and the pressure in the first stage is 1.0 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 100 °C, the heating rate in the second stage is 4 °C / min, the stirring rate in the second stage is 20 r / min, the reaction time in the second stage is 6 h, and the reaction pressure in the second stage is 2.0 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 42 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 80 °C, its yield is calculated to be 39.5%, and its molecular weight is tested to be 255,000, which can be used as a binder, pore expander and emulsion polymerization stabilizer.

[0087] Using the heavy gasoline fraction greater than 80 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor. The catalyst is loaded with ZSM-5 / ZSM-11 eutectic zeolite catalyst (SiO 2 / Al 2 O 3 = 60). The reforming reaction occurs under the conditions of a reaction temperature of 220 °C, a pressure of 1.2 MPa, a mass space velocity of 1.0 h -1 , and a hydrogen flow rate of 50 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 6% and the octane number is 84 (RON).

[0088] Example 6

[0089] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0090] Cut FCC gasoline (olefin content 33%), using the light gasoline fraction less than the cutting temperature of 100 °C as the raw material (olefin mass content 45%), 55.4321 g of light gasoline fraction, 21.0596 g of maleic anhydride, 0.0554 g of initiator (azodiisooctanenitrile), 0.0096 g of auxiliary agent (cashew shell oil) and 166.2918 g of solvent (ethyl acetate) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 50 °C, the heating rate in the first stage is 5 °C / min, the stirring rate in the first stage is 5 r / min, the reaction time in the first stage is 4 h, and the pressure in the first stage is 2.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 120 °C, the heating rate in the second stage is 2 °C / min, the stirring rate in the second stage is 30 r / min, the reaction time in the second stage is 2 h, and the reaction pressure in the second stage is 2.5 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 49 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 100 °C, its yield is calculated to be 39.8%, and its molecular weight is tested to be 125,000, which can be used as a binder, pore-expanding agent and emulsion polymerization stabilizer.

[0091] Using the heavy gasoline fraction with a boiling point above 100 °C obtained by cutting as the raw material, a reforming reaction is carried out in a fixed-bed reactor filled with ZSM-5 / ZSM-11 eutectic molecular sieve catalyst (SiO 2 / Al 2 O 3 = 90). The reforming reaction occurs under the conditions of a reaction temperature of 380 °C, a pressure of 3.5 MPa, a mass space velocity of 1.5 h -1 , and a hydrogen flow rate of 60 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 6% and the octane number is 89 (RON).

[0092] Example 7

[0093] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0094] Cut the FCC gasoline (olefin content 38%), and use the light gasoline fraction with a boiling point below the cutting temperature of 120 °C as the raw material (olefin mass content 47%). The light gasoline fraction is 50.5364 g, maleic anhydride is 28.4265 g, initiator (azodiisooctanenitrile) is 0.6317 g, auxiliary agent (triallyl isocyanurate) is 0.5427 g, solvent (isopropyl acetate 129.4985 g) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 80 °C, the heating rate in the first stage is 10 °C / min, the stirring rate in the first stage is 10 r / min, the reaction time in the first stage is 5 h, and the pressure in the first stage is 0.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 110 °C, the heating rate in the second stage is 3 °C / min, the stirring rate in the second stage is 30 r / min, the reaction time in the second stage is 6 h, and the reaction pressure in the second stage is 2.5 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 37 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 120 °C, its yield is calculated to be 25.3%, and its molecular weight is tested to be 103,000, which can be used as a binder, pore expander and emulsion polymerization stabilizer.

[0095] Using the heavy gasoline fraction with a boiling point higher than 120 °C obtained by cutting as the raw material, a reforming reaction is carried out in a fixed-bed reactor filled with β zeolite catalyst (SiO 2 / Al 2 O 3 = 30). The reforming reaction occurs under the conditions of a reaction temperature of 260 °C, a pressure of 1.0 MPa, a mass space velocity of 1.5 h -1 , and a hydrogen flow rate of 100 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 4% and the octane number is 92 (RON).

[0096] Example 8

[0097] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0098] Cut FCC gasoline (olefin content 36%). Using the light gasoline fraction with a boiling point lower than the cutting temperature of 140 °C as the raw material (olefin mass content 47%), 58.7881 g of light gasoline fraction, 24.4952 g of maleic anhydride, 0.4899 g of initiator (azobisisobutyronitrile), 0.2450 g of auxiliary agent (triallyl isocyanurate) and 128.3538 g of solvent (butyl acetate) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 60 °C, the heating rate in the first stage is 3 °C / min, the stirring rate in the first stage is 6 r / min, the reaction time in the first stage is 0.5 h, and the pressure in the first stage is 2.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 120 °C, the heating rate in the second stage is 4 °C / min, the stirring rate in the second stage is 40 r / min, the reaction time in the second stage is 1 h, and the reaction pressure in the second stage is 2.5 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 40 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 140 °C, its yield is calculated to be 35.8%, and its molecular weight is tested to be 587,000, which can be used as a plastic modifier or an independent material.

[0099] Using the heavy gasoline fraction with a boiling point higher than 140 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor with a ZSM-11 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 300). The reforming reaction occurs under the conditions of a reaction temperature of 320 °C, a pressure of 3.0 MPa, a mass space velocity of 2.0 h -1 , and a hydrogen flow rate of 90 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 4% and the octane number is 91 (RON).

[0100] Example 9

[0101] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0102] Cut FCC gasoline (olefin content 37%). Using the light gasoline fraction with a boiling point lower than the cutting temperature of 150 °C as the raw material (olefin mass content 44%), 50.502 g of light gasoline fraction, 31.8960 g of maleic anhydride, 0.5316 g of initiator (azodiisooctanenitrile), 0.1450 g of auxiliary agent (cashew nut shell oil) and 111.6362 g of solvent (isopentyl acetate) and H 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 70 °C, the heating rate in the first stage is 5 °C / min, the stirring rate in the first stage is 20 r / min, the reaction time in the first stage is 3.5 h, and the pressure in the first stage is 1.5 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 50 °C, the cooling rate in the second stage is 4 °C / min, the stirring rate in the second stage is 50 r / min, the reaction time in the second stage is 2 h, and the reaction pressure in the second stage is 1.5 MPa; after the polymerization is completed, a milky white solid-liquid mixture is obtained. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 31 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 150 °C, its yield is calculated to be 32.5%, and its molecular weight is tested to be 287,000, which can be used as a binder, pore-expanding agent and emulsion polymerization stabilizer.

[0103] Using the heavy gasoline fraction greater than 150 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor, loading MCM-56 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 150), under the conditions of a reaction temperature of 340 °C, a pressure of 0.8 MPa, a mass space velocity of 2.5 h -1 , and a hydrogen flow rate of 120 mL / min, the reforming reaction occurs. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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. The analysis shows that its olefin content is 5% and the octane number is 85 (RON).

[0104] Example 10

[0105] This example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0106] Cut FCC gasoline (olefin content 35%), using the light gasoline fraction less than the cutting temperature of 80 °C as the raw material (olefin mass content 42%), 48.459 g of light gasoline fraction, 10.026 g of maleic anhydride, 0.3342 g of initiator (azodiisooctanenitrile), 0.0985 g of auxiliary agent (1,2-polybutadiene) and solvent (93.576 g of isopropyl acetate) and N 2Dynamic polymerization reaction occurs. In the first-stage polymerization reaction, the reaction temperature in the first stage is 80 °C, the heating rate in the first stage is 2 °C / min, the stirring rate in the first stage is 5 r / min, the reaction time in the first stage is 2 h, and the pressure in the first stage is 2.0 MPa; in the second-stage polymerization reaction, the reaction temperature in the second stage is 60 °C, the cooling rate in the second stage is 2 °C / min, the stirring rate in the second stage is 20 r / min, the reaction time in the second stage is 4 h, and the reaction pressure in the second stage is 2.0 MPa; after polymerization is completed, a milky white solid-liquid mixture is obtained. Through steps such as centrifugation, separation, and drying, a white functional material is obtained. Then, the components of the filtrate mixture are distilled at 46 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for polymerization reaction. Based on the light gasoline fraction at 80 °C, its yield is calculated to be 23.5%, its molecular weight is tested to be 15,000, and it can be used as a binder, pore-expanding agent, and emulsion polymerization stabilizer.

[0107] Using the heavy gasoline fraction greater than 80 °C obtained by cutting as the raw material, a reforming reaction is carried out on a fixed-bed reactor, filled with ZSM-5 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 360). Under the conditions of a reaction temperature of 240 °C, a pressure of 1.0 MPa, a mass space velocity of 4.0 h -1 , and a hydrogen flow rate of 85 mL / min, a reforming reaction occurs. After the reforming reaction, the reformed product of heavy gasoline is blended with the 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 shows that its olefin content is 5% and its octane number is 90 (RON).

[0108] Comparative Example 1

[0109] This comparative example provides a method for producing gasoline with reduced olefins and rich in materials, which includes the following steps:

[0110] Cut FCC gasoline (olefin content 20%). Using the light gasoline fraction with a temperature less than 50 °C lower than the cutting temperature as the raw material (olefin mass content 28%), at a polymerization reaction temperature of 50 °C and a pressure of 0 MPa (N 2 ), except for not adding any additives (cashew shell oil, triallyl isocyanurate, and 1,2-polybutadiene), the raw material ratio is the same as that in Example 4. A polymerization reaction occurs for 12 h to obtain a milky yellow solid, and no white functional material is obtained. Then, the components of the filtrate mixture are distilled at 60 °C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for polymerization reaction. Based on the light gasoline fraction at 50 °C, its yield is calculated to be 11.1%, and its molecular weight is tested to be 2300. The reformed product of heavy gasoline is 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 shows that its olefin content is 6% and its octane number is 80 (RON).

[0111] Comparative Example 2

[0112] This comparative example provides a method for producing gasoline with reduced olefins and rich in materials, which includes the following steps:

[0113] Using the whole fraction of FCC gasoline as raw material without cutting, in a one-stage polymerization reaction, the one-stage reaction temperature is 100 °C, and the one-stage pressure is 0.5 MPa (H 2 ), and the other reaction conditions are the same as those in Example 9. After the polymerization reaction, a milky yellow solid is obtained. Based on the whole fraction of FCC light gasoline as the raw material, its yield is calculated to be 12.5%, and its molecular weight is measured to be 1503. After the reforming reaction of the whole fraction of FCC gasoline, the olefin content is 32%, and the octane number is 84 (RON).

[0114] Comparative Example 3

[0115] This comparative example provides a method for producing gasoline with reduced olefins and rich in functional materials, which includes the following steps:

[0116] Cut FCC gasoline (olefin content 35%), and use the light gasoline fraction with a temperature lower than the cutting temperature of 90 °C as the raw material (olefin mass content 42%). At a polymerization reaction temperature of 200 °C and a pressure of 2.0 MPa (H 2 ), 53.4762 g of light gasoline fraction, 30.8325 g of maleic anhydride, 0.5187 g of initiator (azobisisobutyronitrile), 0.1239 g of auxiliary agent (triallyl isocyanurate), and 102.9815 g of solvent (isopentyl acetate) undergo a polymerization reaction for 12 h to obtain a milky white solid-liquid mixture. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the filtrate mixture components are distilled at 65 °C to obtain light gasoline with a low olefin content and a heavy fraction, and the heavy fraction is recycled for the polymerization reaction. Based on the light gasoline fraction at 90 °C, its yield is calculated to be 20.4%, and its molecular weight is measured to be 1286.

[0117] Using the heavy gasoline fraction obtained by cutting and greater than 90 °C as the raw material, a reforming reaction is carried out on a fixed-bed reactor, loading a ZSM-5 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 90), and a reforming reaction occurs under the conditions of a reaction temperature of 200 °C, a pressure of 2.5 MPa, a hydrogen mass space velocity of 5 h -1 , and a hydrogen flow rate of 60 mL / min. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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 shows that its olefin content is 35% and the octane number is 76 (RON).

[0118] Comparative Example 4

[0119] This comparative example provides a method for reducing olefins in gasoline and enriching functional materials, which includes the following steps:

[0120] Cut FCC gasoline (olefin content 37%) to use the light gasoline fraction below the cutting temperature by 150°C as the raw material (olefin mass content 44%). At a polymerization reaction temperature of 120°C and a pressure of 0.5 MPa (H 2 )), 16.9480 g of light gasoline fraction, 30.5064 g of maleic anhydride, 0.4327 g of initiator (azodiisooctanenitrile), 0.6356 g of auxiliary agent (cashew shell oil), and 43.2174 g of solvent (isopentyl acetate) undergo a polymerization reaction for 10 h to obtain a milky white solid-liquid mixture. After centrifugation, separation, drying and other steps, a white functional material is obtained. Then, the filtrate mixture components are distilled at 20°C to obtain light gasoline with a low olefin content and heavy components, and the heavy components are recycled for the polymerization reaction. Based on the light gasoline fraction at 150°C, its yield is calculated to be 40.2%, and its molecular weight is tested to be 3009.

[0121] Using the heavy gasoline fraction obtained by cutting and greater than 150°C as the raw material, a reaction is carried out in a fixed-bed reactor filled with a ZSM-5 / ZSM-11 molecular sieve catalyst (SiO 2 / Al 2 O 3 = 60). Under the conditions of a reaction temperature of 460°C, a pressure of 0.3 MPa, a mass space velocity of 0.3 h -1 , and a hydrogen flow rate of 80 mL / min, a reforming reaction occurs. After the reforming reaction, the reformed product of the heavy gasoline is blended with the 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 shows that its olefin content is 14% and the octane number is 78 (RON).

[0122] It can be seen from the results of Examples 1-10 and Comparative Examples 1-4 that the present invention first selects an appropriate temperature to cut gasoline into light gasoline and heavy gasoline. For light gasoline, a dynamic polymerization method is adopted, and the polymerization reaction is precisely controlled through two different process technologies to achieve controllable preparation of functional materials with different molecular weights, and then functional materials for different uses are obtained. During the reaction process, the unreacted materials are recycled at the same time to improve the polymerization reaction efficiency; while the heavy gasoline undergoes a reforming reaction under the action of a catalyst to obtain high-quality gasoline blending components with a high octane number and a low olefin content through reactions such as isomerization, alkylation and hydrogen transfer.

Claims

1. A controllable preparation method for reducing olefins in gasoline and rich in functional materials, 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. Make the light gasoline fraction obtained in S1 undergo a dynamic polymerization reaction with maleic anhydride under the action of an initiator, an auxiliary agent, a solvent and a gas through two-stage heating 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 the heavy component is recycled for the polymerization reaction; S4. Make the heavy gasoline fraction obtained by cutting in S1 undergo a reforming reaction under the action of a catalyst; S5. Blend the heavy gasoline reforming 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, preferably 100-120°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; Preferably, the initiator is azobisisobutyronitrile.

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; Preferably, the auxiliary agent is triallyl isocyanurate.

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; Preferably, the solvent is isopentyl acetate.

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 heating 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; Preferably, the first-stage reaction temperature is 40-70°C, the first-stage heating rate is 2-5°C / min, the first-stage stirring rate is 0-10 r / min, the first-stage reaction time is 1-3 h, and the first-stage reaction pressure is 0.5-1.5 MPa.

8. The preparation method according to claim 1, wherein, The conditions for 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; 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 20-50 r / min, the second-stage reaction time is 2-5 h, and the second-stage reaction pressure is 0.5-1.5 MPa.

9. The preparation method according to claim 1, wherein, the olefin content of the FCC gasoline is greater than or equal to 30%, preferably greater than or equal to 34%; Preferably, the olefin content of the light gasoline fraction is greater than or equal to 39%, preferably greater than or equal to 43%.

10. The preparation method according to claim 1, wherein, The conditions for the reforming reaction are as follows: reaction temperature 90 - 380 °C, reaction pressure 0.1 - 5.0 MPa, mass space velocity 0.1 - 5.0 h -1 ; Preferably, the conditions for the reforming reaction are as follows: reaction temperature 150 - 260 °C, pressure 0.5 - 2.5 MPa, mass space velocity 0.5 - 2.0 h -1 .

11. The preparation method according to claim 1, wherein, 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; Preferably, the catalyst is ZSM-5 / ZSM-11 eutectic molecular sieve.

12. The preparation method according to claim 11, wherein, The silicon-aluminum molar ratio of the ZSM-5 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, preferably SiO 2 / Al 2 O 3 = 90 - 270; Preferably, the molar ratio of silicon to aluminum of the ZSM-11 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 120 - 300; Preferably, the silica-alumina molar ratio of the ZSM-5 / ZSM-11 eutectic zeolite is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 120 - 270; Preferably, the molar ratio of silicon to aluminum of the MCM-56 molecular sieve is SiO 2 / Al 2 O 3 = 30 - 400, more preferably SiO 2 / Al 2 O 3 = 150 - 300; Preferably, the molar ratio of silicon to aluminum of the β-zeolite is SiO 2 / Al 2 O 3 = 15 - 300, more preferably SiO 2 / Al 2 O 3 = 30 - 150.

13. The preparation method according to claim 1, wherein, in step S3, the temperature of the distillation is 25-60 °C, more preferably 30-50 °C.

14. A reformulated blended gasoline, which is prepared by the preparation method according to any one of claims 1-13; Preferably, the olefin content of the reformulated blended gasoline is less than 35%, preferably less than 25%; Preferably, the octane number of the reformulated blended gasoline is greater than or equal to 84, preferably greater than 90.

15. A functional material, which is prepared by the preparation method according to any one of claims 1-13; Preferably, the molecular weight distribution range of the functional material is 5,000-600,000, preferably greater than 50,000.

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