A solid acid catalyst and a method for producing long-chain alkylaromatics

Abstract

A solid acid catalyst for producing long-chain alkyl aromatic hydrocarbons, characterized in that the solid acid catalyst is loaded with a noble metal and a non-noble metal, the noble metal being 0.03-0.06% and the non-noble metal being 5-17% based on the weight of the solid acid catalyst.

Description

Technical Field

[0001] This invention relates to a catalyst and a method for producing long-chain alkyl aromatics, and more specifically, to a method for producing long-chain alkyl aromatics by means of a solid acid catalyst and an alkylation reaction of aromatics and long-chain olefins. Background Technology

[0002] Linear alkylbenzenes, obtained by alkylation of benzene and long-chain olefins, are important chemical intermediates in the synthesis of detergents. These intermediates can be further processed through sulfonation, neutralization, and other reactions to yield high-performance anionic surfactants—alkylbenzene sulfonates. The alkylation of benzene and long-chain olefins began in the 1940s, laying the foundation for the synthetic detergent industry.

[0003] Currently, 83% of the world's linear alkylbenzene production uses the HF process, 9% uses the AlCl3 process, and 8% uses the Detal process.

[0004] Both the HF and AlCl3 processes suffer from drawbacks such as high environmental pollution, severe equipment corrosion, difficulty in product separation, and high investment costs. The Detal process, a solid acid process jointly developed by UOP (USA) and CEPSA (Spain), was industrialized in the mid-1990s. The Detal process uses an amorphous silica-alumina catalyst containing fluorine (F). However, its widespread adoption and development are limited by problems such as fluorine loss, discontinuous alkylation reactions and catalyst regeneration, high operating costs, and frequent regeneration. Therefore, developing green and environmentally friendly solid acid alkylation technology is a future trend.

[0005] Studies on the synthesis of straight-chain alkylbenzenes from benzene and long-chain olefins using solid acid catalysis have largely employed molecular sieves and heteropolyacid-type solid acid catalysts. However, the problems of easy deactivation and short single-cycle lifetime of solid acid catalysts have not yet been effectively solved.

[0006] Current research focuses primarily on catalytic materials or process optimization to improve single-cycle uptime, but this approach suffers from several problems, including poor catalytic material performance, frequent process operations, and high costs. For example, CN1043524C discloses a method for benzene alkylation using fluorinated silica-alumina and straight-chain monoolefins. Under alkylation conditions, benzene and straight-chain monoolefins are contacted with a fluorinated silica-alumina catalyst comprising silica and alumina in a weight ratio of 1:1-9:1 and a fluoride content of 1-6 (wt), using C6 to C440 ... 20 Linear monoolefins are used to alkylate benzene, achieving 98% olefin conversion, 85% or better selectivity for the resulting monoalkylbenzene, and at least 90% linearity with respect to the resulting monoalkylbenzene. However, this technology still results in low olefin conversion and causes environmental pollution due to fluoride ion loss.

[0007] CN101535221B discloses a method for preparing alkylbenzenes on a solid acid catalyst with a low benzene to olefin ratio and low heavy matter formation. This method uses small crystals, acidic FAU molecular sieves as the catalyst under alkylation conditions.

[0008] CN111514924A discloses a catalytic synthesis method for long-chain alkyl aromatics, the method comprising: first, feeding the raw material aromatics into a fixed-bed alkylation reactor and filling the reactor; then, feeding the raw material aromatics and raw material C6-C... 24 A mixture of long-chain olefins and additive long-chain alkyl aromatic solvents or long-chain alkane solvents is fed into a fixed-bed reactor and contacted with an SBA-15 type mesoporous molecular sieve alkylation solid acid catalyst to carry out the alkylation reaction of aromatics and long-chain olefins, generating long-chain alkyl aromatics as the product. A portion of the effluent from the alkylation reactor is recycled back to the reactor as circulating fluid, and another portion is sent to the distillation separation system to separate excess feed and product as effluent.

[0009] US5648579A discloses a method for the alkylation reaction of benzene and 1-dodecene using a pulsed feed method. In this method, benzene is continuously fed into the feedstock, while the olefin feed is stopped at intervals to achieve pulsed feed. The molar ratio of benzene to olefin is between 8 and 20, the number of carbon atoms in the straight-chain olefin ranges from 10 to 14, and the pulse feed interval is between 10 and 60 minutes. Summary of the Invention

[0010] Unlike conventional understanding of solid acid catalysts supported on precious and non-precious metals, the inventors of this invention unexpectedly discovered through experimentation that alkylation catalysts with ultra-low loadings of precious metals and high loadings of non-precious metals not only exhibit good alkylation activity for long-chain olefins and aromatics but also good alkylation regeneration activity. This allows for continuous, stable, and long-term operation of the equipment while significantly reducing the amount of precious metals used, thereby lowering production costs. Based on this, this invention was developed.

[0011] Therefore, the object of the present invention is to provide a method for producing long-chain alkyl aromatics that differs from the prior art, and that can significantly reduce the production cost of long-chain alkyl aromatics.

[0012] To achieve the above objectives, the present invention provides a method for producing long-chain alkyl aromatics, characterized in that the aromatics are contacted with long-chain olefins under alkylation reaction conditions and in the presence of a solid acid catalyst, wherein the solid acid catalyst is loaded with noble metals and non-noble metals, and based on the weight of the solid acid catalyst, the noble metals account for 0.03-0.06% and the non-noble metals account for 5-17%.

[0013] In this invention, the noble metal comprises 0.035-0.055%, preferably 0.04-0.05 wt%. The non-noble metal comprises 7-15%, preferably 8-13 wt%. The noble metal is selected from one or more of Pt, Pd, and Ru, with Pt being preferred. Pt can synergistically interact with Brønsted acid and also serve as a source of some Lewis acid centers, thereby improving catalyst lifetime. The non-noble metal is selected from one or more of Mn, Ni, and Cu, with Ni being preferred. More preferably, it is a combination of Pt as the noble metal and Ni as the non-noble metal.

[0014] In this invention, the solid acid catalyst contains 40-95 wt% molecular sieve and 5-60 wt% inorganic oxide.

[0015] The molecular sieve is preferably one or more of mordenite, β-type zeolite, X-type zeolite, and Y-type zeolite. Taking benzene as an example, the deactivation of the alkylation reaction of benzene and long-chain olefins is caused by the blockage of catalyst pores by the heavy alkylbenzenes generated during the reaction. This reaction can be catalyzed by both Brønsted acid and Lewis acid. Therefore, properly controlling the catalyst cell can ensure the integrity of the catalyst crystal structure and ensure sufficient Brønsted acid active centers for the reaction. Therefore, in this invention, the most preferred molecular sieve is a Y-type zeolite with a cell size of 2.448–2.457 nm, preferably 2.452–2.455 nm. Since heavy alkylbenzenes are the key to catalyst deactivation, a certain proportion of mesopores can promote the timely diffusion of macromolecules such as heavy alkylbenzenes from the pores and delay catalyst coking. Therefore, in this invention, the most preferred molecular sieve has a mesopore volume to total pore volume ratio of 0.15–0.29, preferably 0.18–0.26, for the Y-type zeolite. The mesopore volume and total pore volume were determined by static low-temperature nitrogen adsorption capacity analysis (BET) using an ASAP2420 adsorption instrument from Micron Technology, USA. The measurement procedure was as follows: The sample was first dried in an oven at 110℃ for 2 hours to remove surface water. Then, a certain amount of sample was weighed and placed in the degassing unit, and a vacuum was drawn (vacuum degree less than 1.33 Pa). The sample was then treated at 90℃ for 1 hour, followed by heating to 330℃ for 9–10 hours. Nitrogen adsorption-desorption tests were performed on the sample under liquid nitrogen cooling conditions to obtain adsorption-desorption curves. The specific surface area and pore volume were calculated using the BET formula.

[0016] The inorganic oxide is selected from one or more of silicon oxide, aluminum oxide, zirconium oxide, and titanium oxide.

[0017] In a preferred embodiment of the present invention, the solid acid catalyst is obtained by the following steps: (1) mixing molecular sieves and inorganic oxides uniformly to form a solid acid component; (2) dissolving noble metal and non-noble metal precursors in deionized water, adding an alkaline solution to adjust the pH value to not less than 11.5, for example, a solution of 12-14; (3) mixing the solution obtained in step (2) with the solid acid component formed in step (1), thoroughly impregnating at 40-90°C, then performing vacuum low-temperature evaporation until the solid acid component content is at least 80% by weight, drying, and calcining to obtain a solid acid catalyst precursor; (4) reducing the solid acid catalyst precursor obtained in step (3) under a hydrogen-containing atmosphere to obtain a solid acid catalyst. Under thorough impregnation in an alkaline environment, the dissolution of the molecular sieve framework aluminum and its reinsertion into the molecular sieve framework can be achieved.

[0018] In step (2), the alkaline solution is derived from ammonia, sodium hydroxide solution, ethylenediamine, triethylamine, and triethanolamine, or combinations thereof. To achieve sufficient impregnation for aluminum re-insertion, in step (3), the solution obtained in step (2) is mixed with the solid acid component formed in step (1), wherein the mass ratio of the solution to the solid acid component is 1.2–5, preferably 1.8–3, and more preferably 2.0–2.7.

[0019] In this invention, the alkylation reaction involves the contact of aromatic hydrocarbons with long-chain olefins to generate straight-chain alkyl aromatic hydrocarbons.

[0020] The long-chain olefin is C 10 ~C 14 One or more of any long-chain olefins. Examples of such long-chain olefins include: decene, undecene, dodecene, tridecene, tetradecene, and their isomers.

[0021] The aromatic hydrocarbon is one or more monocyclic or polycyclic aromatic hydrocarbons. Preferably, the aromatic hydrocarbon is a monocyclic or bicyclic aromatic hydrocarbon. The total carbon number of the aromatic hydrocarbon is 6 to 18. Preferably, the total carbon number of the aromatic hydrocarbon is 6 to 11; the aromatic hydrocarbon has 0 to 8 side chains, preferably 0 to 6. Examples of the aromatic hydrocarbon include benzene, naphthalene, toluene, xylene, diethylbenzene, trimethylbenzene, tetramethylbenzene, and their isomers. The most preferred aromatic hydrocarbon in this invention is benzene.

[0022] In this invention, the alkylation reaction conditions are 70–280°C, 1.5–4 MPa, and a feed mass hourly space velocity (WHSV) of 1–40 h⁻¹. -1 The molar ratio of aromatics to olefins is 1–100:1. Preferably, the alkylation reaction conditions are: temperature 90–180°C, pressure 2.0–3.0 MPa, and feedstock (aromatics and long-chain olefins) mass hourly space velocity (HHSV) 3–30 h⁻¹. -1 The molar ratio of aromatics is 1 to 80:1.

[0023] In this invention, the solid acid catalyst supported on noble metals and non-noble metals is deactivated and then regenerated by hydrogen. The hydrogen regeneration conditions are a temperature of 90-500°C, a pressure of 0-5 MPa, and a hydrogen flow rate of 20-500 (mL / min / g catalyst).

[0024] The method provided by this invention can be implemented in various reaction apparatuses, such as fluidized beds, fixed beds, and slurry beds. The following description of embodiments of this invention uses a fixed bed as an example, but the application of the method is not limited thereto. Detailed Implementation

[0025] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0026] The present invention will be described in detail below through embodiments. It should be understood that the specific embodiments described herein are only for illustration and explanation of the present invention, but do not limit the scope of the present invention.

[0027] Example 1

[0028] Preparation of solid acid catalysts:

[0029] (1) Y-type zeolite (purchased from Sinopec Catalyst Branch, with a cell constant of 2.448 nm and a mesopore volume to total pore volume ratio of 0.05) and alumina were mixed evenly at a weight ratio of 4:1 to form a solid acid component;

[0030] (2) Dissolve Ni(NO3)2·6H2O and Pt(NH3)4(NO3)2 in deionized water, and add diethylamine solution to adjust the pH value to 12;

[0031] (3) The solution prepared in step (2) is mixed with the solid acid component prepared in step (1) at a mass ratio of 2.5, impregnated at 70°C for 2 hours, and then subjected to vacuum low-temperature evaporation until the solid acid content is 80% by weight. The mixture is then dried at 110°C for 5 hours and calcined at 500°C for 2 hours to obtain a solid acid catalyst precursor.

[0032] (4) The solid acid catalyst precursor obtained in step (3) is reduced under a hydrogen atmosphere to obtain the solid acid catalyst. The solid acid catalyst sample is numbered M1, and the specific physicochemical properties of M1 are shown in Table 1.

[0033] Alkylation reaction:

[0034] The alkylation reaction was carried out in a fixed-bed high-pressure microreactor setup. The feedstocks for the alkylation reaction were benzene and n-dodecene. 5 g of alkylation catalyst M1 was packed into a fixed-bed reactor with an inner diameter of 10 mm and a length of 1 m. The reaction temperature was 120 °C, the reaction pressure was 3 MPa, and the feedstock mass hourly space velocity (WHSV) was 3 h⁻¹. -1 The molar ratio of benzene is 40.

[0035] The results of the alkylation reaction are shown in Table 2.

[0036] The catalyst single-cycle lifetime is determined by the olefin breakthrough time in the alkylation product. The catalyst lifetime refers to the time (h) when the n-dodecene conversion rate of the linear alkylbenzene product is less than 99% after chromatography. The n-dodecene conversion rate is obtained by gas chromatography analysis of the product and calculated by the following formula.

[0037] n-Dodecene conversion rate: x = ((w0 - w)) p ) / w0)×100%

[0038] w0 represents the mass fraction of n-dodecene in the feedstock before the reaction; w p This represents the mass fraction of n-dodecene after the reaction.

[0039] The lifespan of the solid acid catalyst after three regenerations is also determined by the olefin breakthrough time in the alkylation product, i.e., the time (h) when the n-dodecene conversion rate of the linear alkylbenzene product is less than 99% after chromatography; the LAB selectivity of the solid acid catalyst after three regenerations refers to the proportion of LAB in the product to monoalkylbenzene; the 2-LAB selectivity of the solid acid catalyst after three regenerations refers to the proportion of 2-LAB to 2-6-LAB.

[0040] The components in the linear alkylbenzene product were analyzed using an online chromatographic analyzer (Agilent GC-7890B). This invention evaluates the technical effectiveness of the alkylation reaction using two indicators: cycle life and product distribution.

[0041] Comparative Example 1

[0042] This comparative example illustrates the alkylation reaction of benzene and n-dodecene using a Y-type solid acid catalyst without metal support, compared to M1.

[0043] Preparation of solid acid catalyst: Y-type zeolite (purchased from Sinopec Catalyst Branch, cell constant 2.448 nm, mesopore volume to total pore volume ratio 0.05) and alumina were mixed uniformly at a weight ratio of 4:1 to form a solid acid component, i.e., a metal-free solid acid catalyst, sample numbered D1. The specific physicochemical properties of D1 are shown in Table 1.

[0044] Alkylation reaction: Same as in Example 1, the results of the alkylation reaction are shown in Table 2.

[0045] Comparative Example 2

[0046] This comparative example illustrates the alkylation reaction of benzene and n-dodecene using a solid acid catalyst supported only on the noble metal Pt, in contrast to M1.

[0047] The solid acid catalyst was prepared in the same manner as in Example 1, except that in (2), only Pt(NH3)4(NO3)2 was dissolved in deionized water.

[0048] The solid acid catalyst sample, designated D2, contains 0.045% Pt. The specific physicochemical properties of D2 are shown in Table 1.

[0049] Alkylation reaction: Same as in Example 1, the results of the alkylation reaction are shown in Table 2.

[0050] Comparative Example 3

[0051] This comparative example illustrates the alkylation reaction of benzene and n-dodecene using a solid acid catalyst supported only on Ni, compared with M1.

[0052] The preparation of solid acid catalysts is the same as in Example 1, except that in (2), only Ni(NO3)2·6H2O is dissolved in deionized water.

[0053] The solid acid catalyst sample, numbered D3, contains 11% Ni. The specific physicochemical properties of D3 are shown in Table 1.

[0054] Alkylation reaction: Same as in Example 1, the results of the alkylation reaction are shown in Table 2.

[0055] Comparative Example 4

[0056] This comparative example illustrates the alkylation reaction of benzene and n-dodecene using a solid acid catalyst that simultaneously supports noble and non-noble metals, but in proportions outside the scope of this invention, in comparison with M1.

[0057] Preparation of solid acid catalyst: Same as in Example 1.

[0058] The solid acid catalyst sample, designated D4, contains 0.08% Pt and 20% Ni. The specific physicochemical properties of D4 are shown in Table 1.

[0059] Alkylation reaction: Same as in Example 1, the results of the alkylation reaction are shown in Table 2.

[0060] Comparative Example 5

[0061] This comparative example is used to illustrate the alkylation reaction of benzene and n-dodecene using a solid acid catalyst that is simultaneously loaded with noble and non-noble metals, but whose loading ratio is not within the scope of this invention, in comparison with M1.

[0062] Preparation of solid acid catalyst: Same as in Example 1.

[0063] The solid acid catalyst sample, designated D5, contains 0.025% Pt and 3% Ni. The specific physicochemical properties of D5 are shown in Table 1.

[0064] Alkylation reaction: Same as in Example 1, the results of the alkylation reaction are shown in Table 2.

[0065] Table 1

[0066]

[0067] Table 2

[0068]

[0069] As can be seen from the results in Table 2, the technical effect of the benzene and n-dodecene alkylation reaction-regeneration using the solid acid catalyst in Example 1 is significantly better than that of Comparative Example 1 (no metal loading), Comparative Example 2 (only a small amount of noble metal Pt loading), and Comparative Example 3 (only non-noble metal Ni loading), and also better than Comparative Example 4 and Comparative Example 5 (the proportion of noble metal or non-noble metal loading is not within the scope of this invention).

[0070] The specific analysis is as follows: In the alkylation reaction, catalysts without metal loading, such as D1, have no regeneration activity. Catalysts with only a small amount of noble metal or only non-noble metal loading, such as D2 and D3, as well as catalysts with noble metal or non-noble metal loadings not within the scope of this invention, such as D4 and D5, all have significantly poor initial catalyst lifetime, lifetime after 3 regenerations, LAB selectivity, and 2-LAB selectivity.

[0071] The solid acid catalyst of this invention, due to the appropriate loading of a non-noble metal-noble metal mixture, leverages the synergistic effect between the two metals, exhibiting stronger hydrogenolysis performance than a single noble metal. Under the hydrogen regeneration conditions provided by this invention, it has the ability to remove the coking component heavy alkylbenzenes that cause deactivation of the solid acid catalyst due to pore blockage through hydrocracking or saturation. For example, the solid acid catalyst used in this invention, catalyst M1 with a noble metal Pt content of 0.045% and a Ni content of 11%, not only achieves a cycle life of 46 hours, but also exhibits a LAB selectivity as high as 91.6% and a 2-LAB ratio as high as 25.7%.

[0072] Example 2

[0073] The catalyst preparation steps in this embodiment are the same as in Example 1, the difference being the different supported metal contents, namely 0.035% Pt and 15% Ni. The solid acid catalyst sample is numbered M2, and the specific physicochemical properties of M2 are shown in Table 3. Table 3 also lists the specific physicochemical properties of M1.

[0074] The alkylation reaction conditions were the same as those in Example 1, and the alkylation reaction results are shown in Table 4. Table 4 also lists the alkylation reaction results of Example 1 using M1.

[0075] Example 3

[0076] The catalyst preparation steps in this embodiment are the same as in Example 1, except that the supported metal content is different, namely 0.055% Pt and 7% Ni. The solid acid catalyst sample is numbered M3, and the specific physicochemical properties of M3 are shown in Table 3.

[0077] The alkylation reaction conditions were the same as those in Example 1, and the alkylation reaction results are shown in Table 4.

[0078] Example 4

[0079] The catalyst preparation steps in this embodiment are the same as in Example 1, except that the supported metal content is different, namely 0.045% Pt and 11% Ni. The solid acid catalyst sample is numbered M4, and the specific physicochemical properties of M4 are shown in Table 3.

[0080] The alkylation reaction conditions were: reaction temperature 70℃, reaction pressure 1.5 MPa, and feed space velocity 20 h⁻¹. -1 The molar ratio of benzene to olefin was 100. The results of the alkylation reaction are shown in Table 4.

[0081] Example 5

[0082] The solid acid catalyst in this embodiment is the same as sample M4 in Example 4.

[0083] The alkylation reaction conditions were: reaction temperature 180℃, reaction pressure 4 MPa, and feed space velocity 1 h⁻¹. -1 The molar ratio of benzene to olefin was 20. The results of the alkylation reaction are shown in Table 4.

[0084] Example 6

[0085] The catalyst preparation steps in this embodiment are the same as in Example 1, except that the Y-type zeolite is replaced with a "cell constant of 2.452 nm and a mesopore volume to total pore volume ratio of 0.26". The solid acid catalyst sample is designated M5, and its specific physicochemical properties are shown in Table 3.

[0086] The alkylation reaction conditions were the same as those in Example 1, and the alkylation reaction results are shown in Table 4.

[0087] Example 7

[0088] The catalyst preparation steps in this embodiment are the same as in Example 1, except that the Y-type zeolite is replaced with "a cell constant of 2.455 nm and a mesopore volume to total pore volume ratio of 0.18".

[0089] The solid acid catalyst sample is numbered M6, and its specific physicochemical properties are shown in Table 3.

[0090] The alkylation reaction conditions were the same as those in Example 1, and the alkylation reaction results are shown in Table 4.

[0091] Table 3

[0092]

[0093] Table 4

[0094]

[0095] As shown in Table 4, the metal contents within the scope of this invention all exhibit excellent alkylation reaction-regeneration activity for benzene and n-dodecene, such as M2 and M3. By changing different reaction conditions, the single-cycle lifetime and selectivity of the catalyst can be further improved, such as M3 and M4. In addition to the combination of noble and non-noble metals, the specific cell constant and mesoporous ratio of the Y-type zeolite also affect the properties of the active sites in the alkylation reaction and the ease of diffusion of reactants and products. A certain proportion of mesoporous material can promote the timely diffusion of macromolecules such as heavy alkylbenzenes from the channels and delay the coking of the catalyst. Such catalysts have better lifetime and selectivity, such as M5 and M6.

Claims

1. A method for producing long-chain alkyl aromatics, comprising alkylating aromatics with long-chain olefins under alkylation reaction conditions and with a solid acid catalyst, characterized in that, The alkylation reaction conditions are temperature 70-180℃, pressure 1.5-4MPa, raw material mass space velocity 1-40h -1 , the molar ratio of aromatic hydrocarbon to alkene is 1-100:1; the solid acid catalyst is loaded with noble metal and non-noble metal, the noble metal is Pt, the non-noble metal is Ni, the content of noble metal is 0.03-0.06% and the content of non-noble metal is 5-17% based on the weight of the solid acid catalyst; the solid acid catalyst contains 40-95wt% of molecular sieve and 5-60wt% of inorganic oxide, the molecular sieve is Y-type zeolite with unit cell of 2.452-2.457nm and the ratio of mesopore volume to total pore volume of 0.15-0.29; the inorganic oxide is selected from one or more of silicon oxide, aluminum oxide, zirconium oxide and titanium oxide.

2. The production method according to claim 1, characterized in that, The precious metal content is 0.035-0.055%.

3. The production method according to claim 1, characterized in that, The precious metal content is 0.04-0.05%.

4. The production method according to claim 1, characterized in that, The non-precious metals comprise 7-15%.

5. The production method according to claim 1, characterized in that, The non-precious metals are 8-13 wt%.

6. The production method according to claim 1, characterized in that, The solid acid catalyst is obtained by the following steps: (1) mixing molecular sieves and inorganic oxides uniformly to form a solid acid component; (2) dissolving the precursors of the noble metal and the non-noble metal in deionized water, and adding alkaline solution to adjust the pH value to not less than 11.5; (3) mixing the solution obtained in step (2) with the solid acid component formed in step (1), fully impregnating at 40~90°C, and then performing vacuum low-temperature evaporation until the solid acid component content is at least 80% by weight, drying, and calcining to obtain a solid acid catalyst precursor; (4) reducing the solid acid catalyst precursor obtained in step (3) under a hydrogen atmosphere to obtain a solid acid catalyst.

7. The production method according to claim 6, characterized in that, The alkaline solution in step (2) is derived from one or more of ammonia, sodium hydroxide solution, ethylenediamine, triethylamine and triethanolamine.

8. The production method according to claim 1, characterized in that, The long-chain olefin is C 10 ~C 14 One or more of any one of the long-chain olefins.

9. The production method according to claim 8, characterized in that, The long-chain olefin is selected from one or more of decene, undecene, dodecene, tridecene, tetradecene, and their isomers.

10. The method according to claim 1, characterized in that, The alkylation reaction conditions are: temperature 90–160 °C, pressure 2.0–3.0 MPa, and feed mass hourly space velocity (WHSV) 3–30 h⁻¹. -1 The molar ratio of aromatics is 1 to 80:1.

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