CN116265105A - Modified Y-type molecular sieve, preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene - Google Patents

Modified Y-type molecular sieve, preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene Download PDF

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CN116265105A
CN116265105A CN202111540798.5A CN202111540798A CN116265105A CN 116265105 A CN116265105 A CN 116265105A CN 202111540798 A CN202111540798 A CN 202111540798A CN 116265105 A CN116265105 A CN 116265105A
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molecular sieve
type molecular
diethylbenzene
treatment
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赵文广
刘国东
黄延强
张涛
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Dalian Institute of Chemical Physics of CAS
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/084—Y-type faujasite
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
    • C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
    • C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
    • C07C6/126—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of more than one hydrocarbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/32—Reaction with silicon compounds, e.g. TEOS, siliconfluoride
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/36—Steaming
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/37—Acid treatment
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The application discloses a modified Y-type molecular sieve, a preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene, wherein the modified Y-type molecular sieve catalyst is obtained by carrying out hydrothermal treatment, acid treatment and silanization treatment on a NaY-type molecular sieve. The raw materials containing benzene and mixed diethylbenzene are reacted at the reaction temperature of 190-260 ℃ and the reaction pressure of 2.0-5 MPa, and the weight space velocity of liquid phase is 1-8 hours ‑1 And (3) carrying out contact reaction on the benzene/mixed diethylbenzene with a modified Y-type molecular sieve catalyst in a fixed bed reactor under the condition that the weight ratio of the benzene to the mixed diethylbenzene is 1-6 to obtain ethylbenzene. The catalyst has the remarkable characteristics of high diethylbenzene conversion rate and less impurity in ethylbenzene in the process of catalyzing benzene and diethylbenzene transalkylation reaction.

Description

Modified Y-type molecular sieve, preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene
Technical Field
The application relates to a modified Y-type molecular sieve, a preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene, belonging to the field of chemistry and chemical engineering.
Background
Ethylbenzene is an important chemical raw material, which is an indispensable key raw material for producing styrene, and most ethylbenzene manufacturers produce ethylbenzene for the purpose of producing styrene, and a small amount of ethylbenzene is used as a solvent, a diluent, diethylbenzene and the like. About 90% or more of ethylbenzene is used for the production of styrene, which is an important basic organic chemical raw material mainly used for the production of polystyrene and its copolymers such AS ABS, AS, styrene-butadiene rubber and its unsaturated polyesters in the field of high molecular materials, and in addition, styrene is widely used AS an organic reaction intermediate in pharmaceutical, paint, pigment and textile industries. With the increasing demand for styrene monomer, the world's ethylbenzene production capacity is increasing as is the automotive industry, insulator industry, packaging industry and commodity industry.
Industrially, most of ethylbenzene is synthesized by alkylation of benzene with ethylene, and as the demand for styrene increases, ethylbenzene is in short supply. In the ethylbenzene industry, either ethylene or ethanol alkylation processes, produce quantities of diethylbenzene which need to be separated from the product and reacted with benzene over a transalkylation catalyst to produce ethylbenzene. By doing so, the service life of the alkylation catalyst is prolonged, the occurrence of side reactions in the alkylation reaction can be reduced, the yield of ethylbenzene is improved, and the energy consumption is reduced.
The transalkylation of benzene and diethylbenzene to produce ethylbenzene is a catalyst and a number of patents disclose the preparation of transalkylation catalysts, such as:
the method adopted in the patent CN 104230633A is to take polyethylbenzene and benzene as reaction raw materials, and the reaction pressure is 2.0-4.5 MPa and the liquid phase weight airspeed is 1-10 hours at the reaction temperature of 100-260 DEG C -1 Under the condition that the weight ratio of benzene to polyethylbenzene is 1-10, the reaction raw material contacts with a catalyst to generate liquid phase transalkylation reaction to generate ethylbenzene, and the transalkylation catalyst is SiO 2 /Al 2 O 3 The optimal result is 68.35% diethylbenzene conversion rate and 99.15% ethylbenzene selectivity at 10 hours of feeding of the binder-free Y-type molecular sieve with the molar ratio of 3-20.
CN 104230637B discloses a process for liquid phase transalkylation of polyethylbenzene and benzene, the catalyst comprising the following components: a) 30-90 parts of beta-type molecular sieve, b) 10-70 parts of binder, wherein the beta-type molecular sieve raw powder is obtained by ammonia treatment, and the optimal result is that the diethylbenzene conversion rate reaches 78.41%, and the ethylbenzene selectivity reaches 99.65%.
CN 104276922A is prepared with polyethylbenzene and benzene as material and through reaction at 100-260 deg.c and 2.0-4.5 MPa for 1-10 hr -1 Under the condition that the weight ratio of benzene to polyethylbenzene is 1-10, the reaction raw material contacts with a catalyst to generate liquid phase transalkylation reaction to generate ethylbenzene, and the transalkylation catalyst is SiO 2 /Al 2 O 3 The optimal result is that the diethylbenzene conversion rate is 72.11% and the ethylbenzene selectivity is 97.11% when the zeolite is fed for 10 hours, wherein the mole ratio of the zeolite is 5-200.
The diethylbenzene transalkylation catalyst adopted by CN 104230637A is Beta molecular sieve containing binder, the optimal result after the raw powder is reacted stably by ammonia gas is diethylbenzene conversion rate 42.67%, and ethylbenzene selectivity reaches 99.22%.
The CN1310051 adopts a gas phase alkyl transfer process, the active component of the adopted catalyst is ZSM-5 molecular sieve, and the molecular sieve is modified by water vapor treatment and organic acid treatment, so that the performance of the gas phase alkyl catalyst is greatly improved, but the gas phase alkyl transfer reaction requires high reaction temperature, and the xylene/ethylbenzene reaches 750ppm.
The transalkylation catalyst comprises beta zeolite, Y zeolite, ZSM-5 zeolite and the like, and the conversion rate of raw material diethylbenzene or the selectivity of product ethylbenzene is effectively improved by carrying out sexual modification treatment on the zeolite catalyst. However, so far, catalysts which simultaneously increase the conversion of raw diethylbenzene and the selectivity of ethylbenzene as a product and have a low xylene content have been rarely reported.
Disclosure of Invention
The invention provides a catalyst for preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene and a preparation method thereof, wherein the catalyst has high diethylbenzene conversion rate and good ethylbenzene selectivity in the process of catalyzing the reaction of preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene, and solves the problem that the high diethylbenzene conversion rate and the high ethylbenzene selectivity are difficult to be compatible in the prior art.
In one aspect of the present application, a modified Y-type molecular sieve catalyst is provided,
the modified Y-type molecular sieve catalyst is obtained by carrying out hydrothermal treatment, acid treatment and silanization treatment on a NaY-type molecular sieve.
In another aspect of the present application, there is provided a method for preparing the modified Y-type molecular sieve catalyst, the method comprising:
(1) Performing ammonium exchange on the NaY type molecular sieve, and roasting I to obtain an ammonium exchanged catalyst;
(2) Sequentially carrying out hydrothermal treatment and acid treatment on the catalyst obtained in the step (1), and roasting II to obtain the modified Y-type molecular sieve catalyst precursor;
(3) Adding the modified Y-type molecular sieve catalyst precursor obtained in the step (2) into an organic solvent solution containing a silicon source for silanization treatment;
(4) Obtaining the modified Y-type molecular sieve catalyst.
Optionally, repeating the steps (1) to (3) for 1 to 3 times;
preferably, the ammonium exchange times are 2-4 times, the hydrothermal treatment is 1-3 times, the acid treatment is 1-3 times, and the silanization treatment is 1-3 times.
Alternatively, ammonium exchange is performed 3 times, water vapor treatment is performed 2 times, and silylation is performed 2 times.
Optionally, the temperature of the roasting I is 450-650 ℃, and the time of the roasting I is … … - … …;
optionally, the temperature of the roasting I is 450-650 ℃;
optionally, the temperature of the roasting II is 450-650 ℃, and the time of the roasting II is … … - … …;
optionally, the temperature of the roasting II is 500-600 ℃;
optionally, the hydrothermal treatment temperature is 450-700 ℃, and the hydrothermal treatment time is 1-6 h;
optionally, the hydrothermal treatment temperature is 500-600 ℃, and the hydrothermal treatment time is 2-4;
optionally, in the hydrothermal treatment, the concentration of the water vapor is 60-100%, and the mass space velocity of the water vapor is 0.1-1.5 h -1 ；
Optionally, the concentration of the water vapor is 80-100%, and the mass airspeed of the water vapor is 0.2-1 h -1 ；
Optionally, the acid treatment is performed with an organic acid;
optionally, the organic acid is at least one selected from citric acid, oxalic acid, acetic acid and ethylenediamine tetraacetic acid;
optionally, the organic acid is citric acid or oxalic acid;
optionally, the concentration of the organic acid is 0.1-1 mol/L;
optionally, the concentration of the organic acid is 0.2-0.8 mol/L;
optionally, the acid treatment temperature is 50-90 ℃ and the acid treatment time is 1-6 h.
Optionally, the acid treatment temperature is 60-80 ℃ and the acid treatment time is 2-3 h.
Optionally, the silicon source is a siloxane;
optionally, the silicon source is at least one selected from tetraethoxysilane, polymethylhydrosiloxane, polymethylsilicone oil, chloropropyl triethoxysilane and methyltrimethoxysilane;
alternatively, the silicon source is selected from ethyl orthosilicate or polymethylhydrosiloxane.
Optionally, the mass concentration of the silicon source in the organic solvent solution containing the silicon source is 2-8%;
optionally, the mass concentration of the silicon source is 4 to 6 percent
Optionally, the organic solvent is at least one selected from n-hexane, n-heptane, n-octane, cyclohexane, methylcyclohexane, benzene, toluene.
Optionally, the organic solvent is cyclohexane or benzene.
Optionally, the silanization treatment temperature is 50-90 ℃, and the silanization treatment time is 4-10 h.
Optionally, the silanization treatment temperature is 60-80 ℃, and the silanization treatment time is 6-8 h.
As a specific embodiment, the preparation method comprises:
extruding industrial NaY molecular sieve, assistant and dilute nitric acid in certain proportion to form, adding into ammonium salt water solution for exchange under the condition of water bath at certain temperature, washing, filtering, drying and roasting, adding the exchanged catalyst into water vapor atmosphere at certain temperature to treat for certain time, then treating in organic acid solution at certain temperature, roasting, taking out molecular sieve, adding into organic solvent solution containing certain amount of silicon source to treat for certain time at certain temperature, and repeating the process for 1-3 times to obtain the product.
The method conventionally employed in the prior art for extrusion molding of Y-type molecular sieves in the method of the present invention is not particularly limited. For example, the mass fraction of the molecular sieve raw powder is 60-90%, the auxiliary agent is pseudo-boehmite powder, sesbania powder, the dilute nitric acid concentration is 3-6%, and the dosage is 60-90%. The ammonium salt exchange treatment method in the method of the present invention is a method conventionally employed in the prior art, and is not particularly limited. For example, ammonium salt solution with the mass concentration of 3-15% is used for treatment for 1-6 hours at 50-90 ℃, and then the solution is washed, filtered and dried. The ammonium salt is at least one of ammonium nitrate, ammonium chloride, ammonium oxalate and ammonium sulfate.
In yet another aspect of the present application, a process for the liquid phase transalkylation of benzene and diethylbenzene to ethylbenzene is provided,
the method comprises the steps of (1) carrying out contact reaction on a raw material containing benzene and diethylbenzene in a reactor and a catalyst to obtain ethylbenzene;
wherein the catalyst is selected from the modified Y-type molecular sieve catalyst or the modified Y-type molecular sieve catalyst obtained according to the preparation method.
The resulting catalyst can be used in a liquid phase transalkylation process of mixed diethylbenzene components and benzene produced in an alkylation process of producing ethylbenzene from ethylene or ethanol.
Optionally, the mass ratio of benzene to diethylbenzene is 1-6;
optionally, the mass ratio of benzene to diethylbenzene is 2-4;
optionally, the mass airspeed of the raw material is 1 to 8 hours -1 ；
Optionally, the mass airspeed of the raw material is 3 to 6 hours -1 。
Alternatively, the diethylbenzene is a mixed diethylbenzene produced in the production of ethylbenzene by a pure ethylene or ethanol alkylation process.
Optionally, the temperature of the reaction is 190-260 ℃; the pressure of the reaction is 2-5.0 MPa.
Optionally, the temperature of the reaction is 200-240 ℃; the pressure of the reaction is 3-4 MPa.
The beneficial effects that this application can produce include:
because the silanized silicon source can be combined with the hydroxyl on the surface of the molecular sieve, the process can not only occur on the outer surface of the molecular sieve, but also occur in the pore channel, different silanized silicon sources can partially enter the inner surface of the molecular sieve to cover partial original active sites, and the treatment has the advantages that the active centers of the molecular sieve can be dispersed, so that the residence time of reaction materials in the pore channel of the molecular sieve is shortened, the mass transfer process is facilitated, and the occurrence of side reactions is further reduced. The Y-type molecular sieve treated by the method is sequentially subjected to ultrastabilization and silanization treatment and is used for liquid phase transalkylation reaction of benzene and mixed diethylbenzene, so that the conversion rate of diethylbenzene and the selectivity of ethylbenzene can be remarkably improved.
Detailed Description
The present application is described in detail below with reference to examples, but the present application is not limited to these examples.
Unless otherwise indicated, all starting materials in the examples of the present application were purchased commercially.
Example 1
Mixing 30g NaY, 3g sesbania powder, 8g pseudo-boehmite and 25g 5% dilute nitric acid together, extruding to form strips, then placing into a water bath with the temperature of 80 ℃, adding 200g1mol/L ammonium nitrate solution for exchange for 2h, washing, filtering, drying, roasting for 3h at the temperature of 550 ℃, taking out and placing into a reaction tube, and placing into a reaction tube according to the temperature of 6g h -1 Is treated by introducing pure water at a rate of 500 DEG C2h, then in 100ml 60 ℃ 0.2mol/L oxalic acid aqueous solution treatment 2h, filtering, drying, 550 ℃ roasting for 3h, finally in 150g benzene dissolved with 3% ethyl orthosilicate 60 ℃ treatment 6h, drying, 550 ℃ roasting for 3h, finally obtaining the final liquid phase transalkylation catalyst.
Example 2
The remaining conditions were the same as in example 1, except that the number of ammonium exchanges was changed to 3.
Example 3
The other conditions were the same as in example 2 except that the number of water vapor treatments was changed to 2 and the number of oxalic acid treatments was changed to 2, i.e., in the order of ammonium exchange, water vapor treatment, acid treatment, ammonium exchange.
Example 4
The remaining conditions were the same as in example 3, except that the temperature of the water vapor treatment was changed to 600 ℃.
Example 5
The remaining conditions were the same as in example 4, except that the temperature of the oxalic acid treatment was changed to 80 ℃.
Example 6
The remaining conditions were the same [ example 5 ], except that the mass fraction of ethyl orthosilicate in benzene was changed to 5%, and the temperature of the silylation treatment was 80 ℃.
Example 7
The other conditions are the same as in example 6, except that the number of silylation treatments is changed to 2, i.e., one silylation treatment is performed after each water vapor treatment.
Comparative example 1
Mixing 30g NaY, 3g sesbania powder, 8g pseudo-boehmite and 25g 5% dilute nitric acid together, extruding to form strips, then placing into a water bath with the temperature of 80 ℃, adding 200g1mol/L ammonium nitrate solution for exchange for 2h, washing, filtering, drying, roasting for 3h at the temperature of 550 ℃, taking out and placing into a reaction tube, and placing into a reaction tube according to the temperature of 6g h -1 Is treated with pure water at 600 ℃ for 2 hours, then treated with 100ml of 0.2mol/L oxalic acid aqueous solution at 80 ℃ for 2 hours, filtered, dried and baked at 550 ℃ for 3 hours. The final catalyst was exchanged 3 times, 2 times each with steam and acid.
Comparative example 2
The patent CN1310051 adopts a gas phase transalkylation process, the active component of the adopted catalyst is ZSM-5 molecular sieve, the molecular sieve is modified by water vapor treatment and organic acid treatment, the reaction condition is that the temperature is 435 ℃, the reaction pressure is 0.6MPa, and the total space velocity of reactants is 28h -1 The benzene/mixed diethylbenzene molar ratio was 5.
Test case
The catalyst reaction performance was evaluated by using a fixed bed reactor fed from bottom to top, the reactor was a stainless steel pipe having an inner diameter of 10mm and a length of 500mm, 3g of the catalyst was charged into a constant temperature section, the catalysts of examples 1 to 7 and comparative example 1 were charged into the reactor, nitrogen was charged to a certain pressure, the replacement was performed for 2 times and the leak was detected, and after the temperature was raised to the reaction temperature, the transalkylation material was started, the reaction conditions were a temperature of 230℃and a reaction pressure of 3MPa and a liquid weight space velocity of 4 hours -1 The benzene/mixed diethylbenzene weight ratio was 3. After 24h of stable feed reaction, sampling and gas chromatography analysis were carried out. The data are shown in Table 1:
TABLE 1 data on benzene and diethylbenzene transalkylation reactions
Figure BDA0003414239380000071
Figure BDA0003414239380000081
The foregoing description is only a few examples of the present application and is not intended to limit the present application in any way, and although the present application is disclosed in the preferred examples, it is not intended to limit the present application, and any person skilled in the art may make some changes or modifications to the disclosed technology without departing from the scope of the technical solution of the present application, and the technical solution is equivalent to the equivalent embodiments.

Claims (10)

1. A modified Y-type molecular sieve catalyst is characterized in that,
the modified Y-type molecular sieve catalyst is obtained by carrying out hydrothermal treatment, acid treatment and silanization treatment on a NaY-type molecular sieve.
2. A method of preparing the modified Y-type molecular sieve catalyst of claim 1, comprising:
(1) Performing ammonium exchange on the NaY type molecular sieve, and roasting I to obtain an ammonium exchanged catalyst;
(2) Sequentially carrying out hydrothermal treatment and acid treatment on the catalyst obtained in the step (1), and roasting II to obtain the modified Y-type molecular sieve catalyst precursor;
(3) Adding the modified Y-type molecular sieve catalyst precursor obtained in the step (2) into an organic solvent solution containing a silicon source for silanization treatment;
(4) Obtaining the modified Y-type molecular sieve catalyst.
3. The method according to claim 2, wherein,
repeating the steps (1) to (3) for 1 to 3 times;
preferably, the ammonium exchange times are 2-4 times, the hydrothermal treatment is 1-3 times, the acid treatment is 1-3 times, and the silanization treatment is 1-3 times.
4. The method according to claim 2, wherein,
the temperature of the roasting I is 450-650 ℃, and the time of the roasting I is 3-6 h;
the temperature of the roasting II is 450-650 ℃, and the time of the roasting II is 3-6 h;
preferably, the hydrothermal treatment temperature is 450-700 ℃, and the hydrothermal treatment time is 1-6 h;
in the hydrothermal treatment, the concentration of the water vapor is 60-100%, and the mass space velocity of the water vapor is 0.1-1.5.
5. The method according to claim 2, wherein,
the acid treatment is carried out by adopting organic acid;
the organic acid is at least one selected from citric acid, oxalic acid, acetic acid and ethylenediamine tetraacetic acid;
the concentration of the organic acid is 0.1-1 mol/L;
the acid treatment temperature is 50-90 ℃, and the acid treatment time is 1-6 h.
6. The method according to claim 2, wherein,
the silicon source is siloxane;
preferably, the silicon source is at least one selected from tetraethoxysilane, polydimethylhydrosiloxane, polymethylsilicone oil, chloropropyl triethoxysilane and methyltrimethoxysilane;
in the organic solvent solution containing the silicon source, the mass concentration of the silicon source is 2-8%;
preferably, the organic solvent is at least one selected from n-hexane, n-heptane, n-octane, cyclohexane, methylcyclohexane, benzene, toluene.
7. The method according to claim 2, wherein,
the silanization treatment temperature is 50-90 ℃, and the silanization treatment time is 4-10 h.
8. A method for preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene is characterized in that,
the method comprises the steps of (1) carrying out contact reaction on a raw material containing benzene and diethylbenzene in a reactor and a catalyst to obtain ethylbenzene;
wherein the catalyst is selected from the modified Y-type molecular sieve catalyst of claim 1 or the modified Y-type molecular sieve catalyst obtained according to the method of preparation of any of claims 2 to 7.
9. The method of claim 8, wherein the step of determining the position of the first electrode is performed,
the mass ratio of benzene to diethylbenzene is 1-6;
the mass airspeed of the raw material is 1-8 h < -1 >;
preferably, the diethylbenzene is a mixed diethylbenzene produced in the alkylation of pure ethylene or ethanol to produce ethylbenzene.
10. The method of claim 8, wherein the step of determining the position of the first electrode is performed,
the temperature of the reaction is 190-260 ℃; the pressure of the reaction is 2-5.0 MPa.
CN202111540798.5A 2021-12-16 2021-12-16 Modified Y-type molecular sieve, preparation method thereof and application thereof in preparing ethylbenzene by liquid phase transalkylation of benzene and diethylbenzene Pending CN116265105A (en)

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