CN114558611A - Catalyst, preparation method thereof and application thereof in preparation of 2, 6-diisopropyl naphthalene - Google Patents
Catalyst, preparation method thereof and application thereof in preparation of 2, 6-diisopropyl naphthalene Download PDFInfo
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Abstract
The invention discloses a catalyst, a preparation method thereof and application thereof in preparation of 2, 6-diisopropyl naphthalene. Spray drying and forming the slurry containing the molecular sieve, the binder, the rare earth metal salt, the siloxane-based compound and the surfactant, and further treating the slurry by high-temperature water vapor and ammonia gas to prepare the microspherical catalyst; the catalyst is applied to the isopropylation reaction of naphthalene or 2-isopropylnaphthalene to prepare 2, 6-diisopropylnaphthalene, and has excellent performance.
Description
Technical Field
The invention relates to a catalyst, a preparation method thereof and application thereof in preparation of 2, 6-diisopropyl naphthalene, belonging to the field of chemistry and chemical engineering.
Background
2, 6-dialkyl naphthalene is a key raw material for producing high-performance polyester fibers and plastics, and polyethylene naphthalate (PEN) prepared by polymerizing 2, 6-naphthalene dicarboxylic acid and ethylene glycol is a novel polyester material with great potential and application prospect. PEN has unique heat resistance, mechanical property, gas barrier property, chemical stability, radiation resistance and the like, and can be widely applied to the manufacturing industries of electronic components, instruments and meters, insulating materials, films for food packaging, beer bottles, aerospace and the like. The bottleneck of the large-scale application of PEN at present is that the preparation process of the key raw material 2, 6-dialkyl naphthalene is complicated and the production cost is high.
The naphthalene resource is rich in China, and the cheap and rich naphthalene is used for synthesizing the 2, 6-dialkyl naphthalene through alkylation reaction, so that the raw material source can be widened, the additional value of the naphthalene and the methyl naphthalene can be improved, the process route is shortened, and the method is an ideal route for preparing the 2, 6-dialkyl naphthalene. However, since the isomers are numerous and the boiling points of the isomers are close, the separation is very difficult, and therefore how to improve the selectivity of 2, 6-dialkylnaphthalene is the key to realize the preparation of 2, 6-dialkylnaphthalene from naphthalene. As the alkyl reagent, methanol, ethanol, isopropanol, propylene, isopropyl bromide, t-amyl alcohol, cyclohexyl bromide, etc. are usually used. Among them, 2, 6-diisopropyl naphthalene (2,6-DIPN) has better selectivity and easier oxidation, and is considered to be a process route with great industrial prospect. CN1793088A discloses a method for preparing 2,6-DIPN by isopropylation of mordenite molecular sieve, the average conversion rate of a plurality of continuous reactors for the hydroisomerization is more than 90 percent, the average content of the 2,6-DIPN in the product is more than 35 percent, and the selectivity of the 2,6-DIPN in a disubstituted product is 58.37 percent to 66.11 percent. CN107954812A discloses a method for naphthalene alkylation in fixed bed reaction, a silanization modified ZSM 5/ZSM 12 composite molecular sieve is used as a catalyst, and the selectivity of 2,6-DIPN is only 41%. At present, a kettle type reaction or a fixed bed reaction process is mostly adopted in the naphthalene isopropylation process, the catalyst is very easy to deactivate in the reaction process (Journal of Catalysis 220(2003) 265-272), and the continuous preparation of 2,6-DIPN is difficult to realize.
According to one aspect of the present application, there is provided a catalyst for the production of 2, 6-diisopropylnaphthalene;
the catalyst is a microsphere catalyst with the particle size of 10-100 microns;
the catalyst comprises a molecular sieve, a binder, a rare earth metal oxide and silicon dioxide;
in the catalyst, the content of the molecular sieve is 20-60 wt%; the upper limit is 60 wt%, 50 wt%, 40 wt%, 30 wt%; the lower limit is 20 wt%, 30 wt%, 40 wt%, 50 wt%;
the content of the binder is 35-55 wt%; the upper limit is 55 wt%, 50 wt%, 45 wt%, 40 wt%; the lower limit is 35 wt%, 40 wt%, 45 wt%, 50 wt%;
the content of the rare earth metal oxide is 0.5-5.0% by mass of the rare earth metal in the rare earth metal oxide; the upper limit is 5.0 wt%, 4.5 wt%, 4.0 wt%, 3.5 wt%, 3.0 wt%, 2.5 wt%, 2.0 wt%, 1.5 wt%, 1.0 wt%; the lower limit is 0.5 wt%, 1.0 wt%, 1.5 wt%, 2.0 wt%, 2.5 wt%, 3.0 wt%, 3.5 wt%, 4.0 wt%, 4.5 wt%;
the content of the silicon dioxide is 1-10%, and the upper limit is 10 wt%, 9 wt%, 8 wt%, 7 wt%, 6 wt%, 5 wt%, 4 wt%, 3 wt%; the lower limit is 2 wt%, 3 wt%, 4 wt%, 5 wt%, 6 wt%, 7 wt%, 8 wt%, 9 wt%;
the molecular sieve is selected from at least one of MOR, MCM-22, MCM-49 or SAPO-5;
the binder is selected from at least one of silica sol, alumina sol, kaolin or sepiolite;
the rare earth metal oxide is at least one of lanthanum oxide, cerium oxide, praseodymium oxide or samarium oxide.
According to another aspect of the present application, there is provided a method for preparing the catalyst, which at least comprises the following steps:
i) mixing raw materials containing a molecular sieve, a binder, a siloxane-based compound, a rare earth metal precursor, a surfactant and water to obtain slurry, spray-drying, and roasting at high temperature to obtain microspheres;
ii) treating the microspheres with mixed gas of high-temperature steam and ammonia gas to prepare the microsphere catalyst.
The rare earth metal precursor is selected from at least one of nitrate, sulfate or hydrochloride of lanthanum, cerium, praseodymium and samarium;
the siloxane-based compound is selected from at least one of compounds with the structure of formula I;
wherein R is1、R2、R3And R4Selected from alkyl with 1-10 carbon atoms;
the surfactant is at least one of sodium hexadecylbenzene sulfonate, polyethylene glycol and sodium dodecyl benzene sulfonate;
the mass content of solids in the slurry is 30-50 wt%, wherein the mass of the rare earth metal precursor is calculated by the mass of an oxide corresponding to a rare earth metal element, and the mass of the siloxane-based compound is calculated by the mass of silicon dioxide generated by decomposition;
the mass content of the surfactant in the solid is 1-5 wt%, and the upper limit is 5 wt%, 4 wt%, 3 wt% or 2 wt%; the lower limit is 1 wt%, 2 wt%, 3 wt%, 4 wt%;
the high-temperature roasting temperature is 400-700 ℃; the upper limit is 700 ℃, 600 ℃ and 500 ℃; the lower limit is 400 ℃, 500 ℃ and 600 ℃;
the high-temperature roasting time is 4-12 hours, and the upper limit is 12 hours, 11 hours, 10 hours, 9 hours, 8 hours, 7 hours, 6 hours and 5 hours; the lower limit is 4h, 5h, 6h, 7h, 8h, 9h, 10h and 11 h.
The temperature of the mixed gas treatment of the water vapor and the ammonia gas is 300-1000 ℃, and the upper limit is 1000 ℃, 900 ℃, 800 ℃, 700 ℃, 600 ℃, 500 ℃ and 400 ℃; the lower limit is 300 deg.C, 400 deg.C, 500 deg.C, 600 deg.C, 700 deg.C, 800 deg.C, 900 deg.C;
the treatment time of the mixed gas of the water vapor and the ammonia gas is 30 min-6 h;
the volume fraction of ammonia in the mixed gas is 20-90%.
According to another aspect of the present application, there is provided a method for preparing 2, 6-diisopropylnaphthalene, comprising at least the steps of:
contacting raw materials containing a naphthalene source and an alkylating agent with a catalyst for reaction to obtain a product containing 2, 6-diisopropyl naphthalene;
the catalyst is selected from the catalysts or the catalysts prepared by the preparation method.
The naphthalene source is selected from naphthalene or/and 2-isopropylnaphthalene; the naphthalene source is molten;
the alkylating agent is selected from propylene or/and isopropanol;
the mass of the catalyst is 2-20 wt% of that of the naphthalene source.
The reaction temperature is 150-300 ℃;
the reaction pressure is 0.1-10 MPa;
the reaction pressure is 0.4-6.0 MPa;
the reaction is carried out in a tank reactor, a loop reactor, a tubular reactor.
The beneficial effects that this application can produce include:
1) the catalyst with the size of 20-100 microns is prepared by spray drying, has high strength, is easy to separate from materials after reaction, and is suitable for batch tank reactors, continuous tank reactors, loop reactors and tubular reactors.
2) The passivation of the acid sites on the outer surface of the catalyst is realized in the spray drying process, and the catalyst has excellent performance in the naphthalene or 2-isopropyl naphthalene isopropylation reaction.
3) The operation method provided by the invention is simple, convenient to operate, low in cost and has potential economic benefits.
Detailed Description
The present invention will be described in detail with reference to examples, but the present invention is not limited to these examples.
The raw materials in the examples of the present invention were all purchased from commercial sources unless otherwise specified.
The analytical methods and conversion, selectivity in the examples were calculated as follows:
qualitative and quantitative analysis of the product is performed by offline operation of Agilent 7890A gas chromatograph, separation by Agilent HP-INNOWAX capillary column, and detection and analysis by hydrogen Flame Ionization Detector (FID).
Naphthalene/2-isopropylnaphthalene conversion ═ converted (moles of naphthalene + 2-isopropylnaphthalene)/(total moles of naphthalene + 2-isopropylnaphthalene) × 100
DIPN selectivity ═ 100 moles of DIPN in product/total moles of product;
2-IPN selectivity is 100 moles of 2-IPN in product/total moles of product;
2,6-DIPN selectivity ═ moles of 2,6-DIPN in product/moles of DIPN in product 100;
the ion ratios in the examples are molar ratios unless otherwise specified.
Example 1 catalyst preparation
Taking 0.10Kg La (NO)3)3·6H2O and 0.10Kg of polyethylene glycol (molecular weight 4000) are dissolved in 3.00Kg of water, and then 1.0Kg of MOR molecular sieve (Si/Al 120), 1.0Kg of kaolin, 5.0Kg of alumina sol (20%) and 0.80Kg of tetraethyl silicate are added and mixed uniformly, and stirred for 30min to prepare a slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-50 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 60min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-01.
Example 2 catalyst preparation
Taking 0.20Kg La (NO)3)3·6H2O and 0.12Kg of polyethylene glycol (molecular weight 4000) were dissolved in 3.00Kg of water, and 1.00Kg of MOR molecular sieve (Si/Al 120), 1.00Kg of kaolin, 5.00Kg of alumina sol (20%) and 0.90Kg of isobutyltriethoxysilane were added and mixed uniformly, followed by stirring for 30min to prepare a slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-50 microns, the mixture is roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, microspheres are prepared, and the measured abrasion index is 1.1.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 60min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-02.
Example 3 catalyst preparation
Taking 0.50Kg La (NO)3)3·6H2O and 0.15Kg of polyethylene glycol (molecular weight 4000) are dissolved in 3.00Kg of water, 1.00Kg of SAPO-5 molecular sieve (Si/(Si + P + Al) ═ 0.20, molar ratio), 1.00Kg of kaolin, 5.00Kg of alumina sol (20%), 0.50Kg of tetrapropyl silicate are added, mixed uniformly, stirred for 30min to prepare slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-50 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.1.
Placing 250g of microspheres in a tube furnace, heating to 600 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-03.
Example 4 catalyst preparation
Taking 0.02Kg La (NO)3)3·6H2O and 0.15Kg of polyethylene glycol (molecular weight 4000) are dissolved in 3.00Kg of water, 1.00Kg of SAPO-5 molecular sieve (Si/(Si + P + Al) ═ 0.20, molar ratio), 1.00Kg of sepiolite, 3.20Kg of silica sol (30%) and 1.20Kg of tetrapropyl silicate are added, mixed uniformly, stirred for 30min to prepare slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-50 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2.
Placing 250g of microspheres in a tube furnace, heating to 400 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-04.
EXAMPLE 5 catalyst preparation
Taking 0.40Kg La (NO)3)3·6H2O, 0.10Kg of hexadecylTrimethyl ammonium bromide is dissolved in 3.00Kg of water, 1.00Kg of MOR molecular sieve (Si/Al is 120), 1.00Kg of sepiolite, 3.20Kg of silica sol (30%) and 0.125Kg of tetrapropyl silicate are added, mixed uniformly and stirred for 30min to prepare slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-100 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2.
Placing 250g of microspheres in a tube furnace, heating to 800 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-05.
Example 6 catalyst preparation
Taking 0.20Kg La (NO)3)3·6H2O and 0.10Kg of cetyltrimethylammonium bromide were dissolved in 3.00Kg of water, and 1.50Kg of MOR molecular sieve (Si/Al 120), 1.00Kg of sepiolite, 1.60Kg of silica sol (30%) and 1.00Kg of tetraethyl silicate were added, mixed uniformly, stirred for 30min to prepare a slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-100 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-06.
Example 7 catalyst preparation
Taking 0.20KgCe (NO)3)3·6H2O and 0.12Kg of cetyltrimethylammonium bromide were dissolved in 3.00Kg of water, and 1.50Kg of MOR molecular sieve (Si/Al is 10), 1.00Kg of sepiolite, 1.60Kg of silica sol (30%) and 1.00Kg of tetraethyl silicate were added and mixed uniformly, and stirred for 30min to prepare a slurry.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-100 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2. Shearing with colloid mill for 30 min.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-07.
Example 8 catalyst preparation
Taking 0.20Kg La (NO)3)3·6H2O and 0.15Kg of polyethylene glycol (molecular weight 20000) are dissolved in 3.00Kg of water, and 1.50Kg of MOR molecular sieve (Si/Al is 10), 5.00Kg of silica sol (30%) and 1.10Kg of tetraethyl silicate are added, mixed uniformly and stirred for 30min to prepare slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-100 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-08.
Example 9 catalyst preparation
Taking 0.20Kg of Pr (NO)3)3·6H2O and 0.04Kg of polyethylene glycol (molecular weight 4000) are dissolved in 3.00Kg of water, and 1.00Kg of MOR molecular sieve (Si/Al is 120), 1.00Kg of kaolin, 5.00Kg of alumina sol (20%) and 1.00Kg of tetraethyl silicate are added and mixed uniformly, and stirred for 30min to prepare slurry.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-50 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.2. Shearing with colloid mill for 30 min.
Placing 250g of microspheres in a tube furnace, heating to 500 ℃ under the protection of nitrogen, stopping introducing nitrogen, injecting 25% ammonia water with the introduction amount of 500g/h, treating for 120min, switching the feeding to nitrogen purging for 30min, and cooling. The resulting catalyst was named NPC-09.
Comparative example 1 catalyst preparation
0.15Kg of polyethylene glycol (molecular weight 4000) was dissolved in 3.00Kg of water, and 1.00Kg of MOR molecular sieve (Si/Al 120), 1.00Kg of kaolin, and 5.00Kg of alumina sol (20%) were added and mixed well, and stirred for 30min to prepare a slurry. Shearing with colloid mill for 30 min.
Spray drying and forming are adopted, the atomization temperature is 380 ℃, the particle size distribution is 20-80 microns, the microspheres are roasted for 6 hours in a muffle furnace at the temperature of 600 ℃, and the measured abrasion index is 1.0. Was named NPC-010.
11-23 evaluation of the reaction Performance of the catalyst Using a high-pressure reactor
A500 mL reaction vessel was used for the evaluation. 250g of catalyst is loaded into a tubular furnace, activated for 240min at 500 ℃ under the protection of inert gas nitrogen, and cooled to room temperature. Taking out the catalyst, adding the catalyst into a batching kettle, adding 5000g of industrial naphthalene, uniformly stirring, replacing with inert gas nitrogen for three times, sealing the reaction kettle, and heating to 100 ℃.
200g of inert solvent is filled into the high-pressure autoclave, the high-pressure autoclave is sealed after being replaced by nitrogen, the temperature is raised to 200 ℃, the nitrogen is punched to 3.0MPa, then slurry and propylene are respectively injected, the slurry feeding speed is 50g/h, the propylene feeding speed is 32.5g/h, the gas is discharged out of the reaction kettle after being condensed, and materials carried in the gas are refluxed through a condenser. And when the total mass in the reaction kettle reaches 300g, overflowing and discharging. The reaction was continued. The reaction was continued for 24h and samples were taken for analysis.
And (3) analysis: taking 5.0g of reaction liquid, diluting by 10 times by adopting cyclohexane, adding 1.0g of n-dodecane serving as an analysis internal standard substance, slowly stirring for 30s to uniformly mix the liquid, sucking the mixed liquid by using a disposable syringe, filtering by using a filter membrane, and transferring to a chromatographic analysis bottle for subsequent analysis.
As shown in Table 2, in the method for preparing 2, 6-diisopropyl naphthalene by alkylation of naphthalene and propylene in each example of the invention, higher naphthalene conversion rate and 2,6-DIPN selectivity are obtained. The naphthalene conversion rate can reach more than 90 percent, and the selectivity of 2,6-DIPN is more than 75 percent.
Although the present application has been described with reference to a few embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the application as defined by the appended claims.
Claims (10)
1. A catalyst is characterized in that the catalyst is used for preparing 2, 6-diisopropyl naphthalene,
the catalyst is a microsphere catalyst with the particle size of 10-100 microns;
the catalyst comprises a molecular sieve, a binder, a rare earth metal oxide and silicon dioxide;
in the catalyst, the content of the molecular sieve is 20-60 wt%;
the content of the binder is 35-55 wt%;
the content of the rare earth metal oxide is 0.5-5.0% by mass of the rare earth metal in the rare earth metal oxide;
the content of the silicon dioxide is 1-10%.
2. The catalyst of claim 1,
the molecular sieve is selected from at least one of MOR, MCM-22, MCM-49 or SAPO-5;
the binder is selected from at least one of silica sol, alumina sol, kaolin or sepiolite;
the rare earth metal oxide is at least one of lanthanum oxide, cerium oxide, praseodymium oxide or samarium oxide.
3. A method for preparing a catalyst according to claim 1 or 2, characterized in that it comprises at least the following steps:
i) mixing raw materials containing a molecular sieve, a binder, a siloxane-based compound, a rare earth metal precursor, a surfactant and water to obtain slurry, spray-drying, and roasting at high temperature to obtain microspheres;
ii) treating the microspheres with mixed gas of high-temperature steam and ammonia gas to prepare the microsphere catalyst.
4. The method for preparing a catalyst according to claim 3,
the rare earth metal precursor is selected from at least one of nitrate, sulfate or hydrochloride of lanthanum, cerium, praseodymium and samarium;
the siloxane-based compound is selected from at least one of compounds with the structure of formula I;
wherein R is1、R2、R3And R4Selected from alkyl with 1-10 carbon atoms;
the surfactant is at least one of sodium hexadecylbenzene sulfonate, polyethylene glycol or sodium dodecyl benzene sulfonate.
5. The method for preparing a catalyst according to claim 3,
the mass content of solids in the slurry is 30-50 wt%, wherein the mass of the rare earth metal precursor is calculated by the mass of an oxide corresponding to a rare earth metal element, and the mass of the siloxane-based compound is calculated by the mass of silicon dioxide generated by decomposition;
the mass content of the surfactant in the solid is 1-5 wt%.
6. The method for preparing a catalyst according to claim 3,
the high-temperature roasting temperature is 400-700 ℃;
the high-temperature roasting time is 4-12 h.
7. The method for preparing a catalyst according to claim 3,
the temperature of the mixed gas treatment of the water vapor and the ammonia gas is 300-1000 ℃;
the treatment time of the mixed gas of the water vapor and the ammonia gas is 30 min-6 h;
the volume fraction of ammonia in the mixed gas is 20-90%.
8. A preparation method of 2, 6-diisopropyl naphthalene is characterized by at least comprising the following steps:
contacting raw materials containing a naphthalene source and an alkylating agent with a catalyst for reaction to obtain a product containing 2, 6-diisopropyl naphthalene;
the catalyst is selected from the catalyst described in claim 1 or 2 or the catalyst prepared by the preparation method described in any one of claims 3 to 7.
9. The method of claim 8, wherein the naphthalene source is selected from naphthalene and/or 2-isopropylnaphthalene;
the naphthalene source is molten;
the alkylating agent is selected from propylene or/and isopropanol;
the mass of the catalyst is 2-20 wt% of that of the naphthalene source.
10. The method according to claim 8,
the reaction temperature is 150-300 ℃;
the pressure of the reaction is 0.1-10 MPa;
preferably, the pressure of the reaction is 0.4-6.0 MPa;
the reaction is carried out in a tank reactor, a loop reactor, a tubular reactor.
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