CN109384637B

CN109384637B - Method for preparing ethylbenzene by benzene and ethylene liquid phase alkylation

Info

Publication number: CN109384637B
Application number: CN201710661832.1A
Authority: CN
Inventors: 陈俊文; 孙明毅; 王永睿; 余少兵; 慕旭宏; 舒兴田
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2017-08-04
Filing date: 2017-08-04
Publication date: 2021-06-11
Anticipated expiration: 2037-08-04
Also published as: CN109384637A

Abstract

The invention relates to a method for preparing ethylbenzene by benzene and ethylene liquid phase alkylation, which adopts a catalyst containing a molecular sieve with a new structure, and has higher reaction activity and better ethylbenzene selectivity. Wherein the new molecular sieve has a schematic chemical composition represented by the formula "first oxide-second oxide" or the formula "first oxide-second oxide-organic templating agent-water", wherein the molar ratio of the first oxide to the second oxide is from 5 to ∞; the molar ratio of water to the first oxide is from 5 to 50; the molar ratio of the organic template to the first oxide is from 0.02 to 0.5, and the molecular sieve has a unique X-ray diffraction pattern.

Description

Method for preparing ethylbenzene by benzene and ethylene liquid phase alkylation

Technical Field

The invention relates to a method for preparing ethylbenzene by liquid phase alkylation of benzene and ethylene, in particular to a method for preparing ethylbenzene by liquid phase alkylation of benzene and ethylene under the catalysis of a novel molecular sieve.

Background

Ethylbenzene is an important organic chemical raw material, and is mainly used for producing styrene monomers so as to synthesize various high polymer materials such as engineering plastics, synthetic resins, synthetic rubbers and the like. Industrially, ethylbenzene is mainly prepared by taking benzene and ethylene as raw materials and carrying out alkylation reaction under the action of a catalyst. The progress of the ethylbenzene synthesis technology has very important significance, and the key point is to develop an alkylation catalyst with high reaction activity and ethylbenzene selectivity.

The ethylbenzene alkylation process mainly comprises an aluminum trioxide liquid phase catalysis method, a molecular sieve gas phase catalysis method and a molecular sieve liquid phase catalysis method. Among them, the liquid phase catalysis method of aluminum trioxide started before the 70 s, and due to the strong corrosivity, the method brings great inconvenience to the equipment maintenance and the product separation, and is not basically adopted at present. Therefore, the development of an environmentally friendly solid acid catalyst is particularly urgent.

In 1976, Mobil and Badger collaborated to develop a ZSM-5 molecular sieve catalyst for the gas phase synthesis of ethylbenzene, and was commercialized in 1980. The Mobil/Badger process is a representative of a gas phase method and is characterized in that the yield of ethylbenzene reaches 99.5 percent; the corrosion and pollution are avoided, and the energy consumption is low; the space velocity of the ethylene is high and reaches 0.4h^-1～6h^-1(ii) a The total service life of the catalyst is more than 2 years, and the investment ratio of the device is AlCl₃The method is low. The disadvantages are high reaction temperature (generally 350-450 ℃), high requirements on equipment and operation process, high energy consumption, a large amount of reaction byproducts, low ethylbenzene selectivity and easy coking and inactivation of the used catalyst; in addition, the ethylbenzene produced by the reaction has impurity xylene of about 800 mu g/g (the xylene content in the ethylbenzene is required to be less than 100 mu g/g industrially), so that the quality of the subsequent polystyrene product is greatly influenced.

The liquid phase method makes the raw material benzene in liquid phase by means of higher pressure, and in the process of alkylating benzene and ethylene, ethylene exists in the reactor in liquid phase form, belonging to the liquid-solid two-phase reaction type, and having a very mature technology at home and abroad. The foreign liquid phase method ethylene ethylbenzene preparing process mainly comprises an EB One process of Lummus/UOP, an EB Max process of Mobil/Badger and a new circulating fixed bed reactor process of the domestic petrochemical engineering scientific research institute. The reaction temperature is 150-300 ℃, the reaction pressure is 3.5-4 MPa, the benzene-olefin ratio is 2-15, and the weight space velocity of ethylene is 0.1h^-1～4.4h^-1. The reaction temperature is easy to control, the catalyst has good stability and long service life, the regeneration period reaches 5 years, and the total service life reaches more than 10 years. Because of low reaction temperature, the equipment can be fully adoptedThe investment cost is relatively low by using carbon steel. The selectivity of the generated ethylbenzene is high, the content of dimethylbenzene in the product ethylbenzene can be reduced to 10 ppm-50 ppm, and the industrial requirements for producing food-grade polystyrene can be completely met.

The active components of the prior catalyst for preparing ethylbenzene by a liquid phase method mainly comprise a Y molecular sieve, a beta molecular sieve and an MCM-22 molecular sieve. Wherein the beta molecular sieve has the highest catalytic activity, and the ethylbenzene selectivity can reach about 93 percent; the selectivity of the MCM-22 molecular sieve is relatively better; whereas Y-type molecular sieves are relatively less selective.

Disclosure of Invention

The present inventors have assiduously studied on the basis of the prior art and have found a novel molecular sieve and further found that the molecular sieve performs well in catalyzing the alkylation reaction of benzene and ethylene, thereby completing the present invention.

In particular, the present invention relates to the following aspects:

1. a process for the liquid phase alkylation of benzene with ethylene to produce ethylbenzene comprising the contact reaction of ethylene and benzene under alkylation reaction conditions in the presence of a catalyst, characterized in that the catalyst comprises a molecular sieve having a chemical composition represented by the formula "first oxide-second oxide" or "first oxide-second oxide-organic templating agent-water", wherein the molar ratio of the first oxide to the second oxide is from 5 to ∞ (preferably from 30 to 150, more preferably from 40 to 120); the first oxide is selected from at least one of silicon dioxide, germanium dioxide, tin dioxide, titanium dioxide and zirconium dioxide (preferably silicon dioxide or a combination of silicon dioxide and germanium dioxide), and the second oxide is selected from at least one of aluminum oxide, boron oxide, iron oxide, gallium oxide, rare earth oxide, indium oxide and vanadium oxide (preferably aluminum oxide); the molar ratio of water to the first oxide is from 5 to 50 (preferably from 5 to 15); the molar ratio of the organic templating agent to the first oxide is from 0.02 to 0.5 (preferably from 0.05 to 0.5, from 0.15 to 0.5, or from 0.3 to 0.5), and has an X-ray diffraction pattern substantially as shown in the following Table,

2. the alkylation process for ethylbenzene according to any preceding claim wherein the X-ray diffraction pattern further comprises X-ray diffraction peaks substantially as shown in the following Table,

3. the alkylation process for ethylbenzene according to any preceding claim wherein the X-ray diffraction pattern further comprises X-ray diffraction peaks substantially as shown in the following Table,

4. the method for preparing ethylbenzene by alkylation according to any one of the preceding claims, wherein the ethylene raw material is one or more of pure ethylene, refinery catalytic cracking dry gas containing ethylene (preferably the volume fraction of ethylene is 10-60%) and refinery catalytic cracking dry gas containing ethylene (preferably the volume fraction of ethylene is 10-60%).

5. The alkylation process for ethylbenzene production according to any of the preceding claims, wherein the catalyst consists of a binder (alumina and/or silica) and the molecular sieve ((preferably the mass fraction of the molecular sieve being 10% to 95% based on the mass of the catalyst)).

6. A process for the alkylation of ethylbenzene according to any of the preceding claims wherein the catalyst is prepared by: mixing and kneading the molecular sieve raw powder, a silicon-containing compound and/or an aluminum-containing compound, nitric acid and deionized water for molding, drying, then burning out a template agent in air at 450-550 ℃, then exchanging in an ammonium salt aqueous solution at 80-90 ℃, and finally roasting and deaminating at 500-600 ℃ for 1-5 hours to obtain a catalyst; wherein the silicon-containing compound is selected from one or more of silica sol, methyl orthosilicate and ethyl orthosilicate, and the aluminum-containing compound is selected from one or more of pseudo-boehmite, SB powder, aluminum sol and aluminum isopropoxide; the ammonium salt is selected from one or more of ammonium nitrate, ammonium chloride and ammonium sulfate.

7. A process according to claim 6, wherein a mixture of a silicon-containing compound and an aluminium-containing compound is used in a molar ratio of from 1:1 to 1:2, based on silicon oxide to aluminium oxide.

8. The process according to claim 1, characterized in that it is carried out in a fixed bubble-bed reactor (preferably with both ethylene and benzene fed from the lower part of the reactor and the reaction products withdrawn from the upper part of the reactor), a fixed trickle-bed reactor or a slurry-bed reactor; and/or

The alkylation reaction conditions are as follows: the reaction temperature is 150-280 ℃, the reaction pressure is 1-4 MPa, and the molar ratio of benzene to ethylene is 1: 1-15: 1, weight hourly space velocity in terms of ethylene of 0.1h^-1～0.8h^-1(the preferable alkylation conditions are that the reaction temperature is 160-250 ℃, the reaction pressure is 1.2-3.6 MPa, the molar ratio of benzene to ethylene is 3: 1-12: 1, and the weight hourly space velocity counted by ethylene is 0.1h^-1～0.5h^-1)。

9. A process for the liquid phase alkylation of benzene with ethylene to produce ethylbenzene comprising the step of contacting ethylene and benzene under alkylation reaction conditions in the presence of a catalyst, wherein the catalyst comprises a molecular sieve produced by the process comprising: contacting under crystallization conditions a first source of oxide, a second source of oxide, optionally a source of base, an organic templating agent, and water to obtain said molecular sieve; wherein, optionally, a step of calcining the obtained molecular sieve is included; the organic template comprises a compound represented by the following formula (I),

wherein the radical R₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight or branched alkylene and C_3-12Straight-chain or branched oxaalkylene, preferably independently of one another, selected from C_3-12Straight chain alkylene and C_3-12Straight oxaalkylene, or preferably one of them is selected from C_3-12Linear or branched alkylene, the other being selected from C_3-12Straight or branched alkylene and C_3-12Straight or branched oxaalkylene, more preferably one selected from C_3-12Linear alkylene and the other is selected from C_3-12Straight chain alkylene and C_3-12Straight oxaalkylene, particularly preferably one selected from C_3-12Linear alkylene and the other is selected from C_4-6Straight chain alkylene and C_4-6Straight-chain oxaalkylene (preferably C)_4-6A straight chain monooxyheteroalkylene group, more preferably- (CH)₂)_m-O-(CH₂)_m-, in which the individual values m, which are identical or different from one another, each independently represent 2 or 3); a plurality of radicals R, equal to or different from each other, each independently selected from C_1-4A linear or branched alkyl group, preferably each independently selected from methyl and ethyl, more preferably both methyl; x is OH.

10. The alkylation process for ethylbenzene according to any of the preceding claims wherein the first oxide source is selected from at least one of a silica source, a germanium dioxide source, a tin dioxide source, a titanium dioxide source and a zirconium dioxide source, preferably a silica source or a combination of a silica source and a germanium dioxide source, and the second oxide source is selected from at least one of an alumina source, a boron oxide source, an iron oxide source, a gallium oxide source, a rare earth oxide source, an indium oxide source and a vanadium oxide source, preferably an alumina source.

11. A process for the alkylation of ethylbenzene according to any of the preceding claims wherein the crystallization conditions comprise: a crystallization temperature of from 80 ℃ to 120 ℃, preferably from 120 ℃ to 170 ℃ or from 120 ℃ to 200 ℃, a crystallization time of at least 1 day, preferably at least 2 days, preferably from 3 days to 8 days, from 5 days to 8 days or from 4 days to 6 days, and the calcination conditions comprise: the calcination temperature is from 300 ℃ to 750 ℃, preferably from 400 ℃ to 600 ℃, and the calcination time is from 1 hour to 10 hours, preferably from 3 hours to 6 hours.

12. The alkylation process for ethylbenzene according to any of the preceding claims wherein the molar ratio of the first oxide source (based on the first oxide) to the second oxide source (based on the second oxide) is from 5 to ∞, preferably from 25 to 95, more preferably from 30 to 70; the molar ratio of water to said first source of oxide (based on said first oxide) is from 5 to 50, preferably from 5 to 15; the molar ratio of the organic templating agent to the first oxide source (based on the first oxide) is from 0.02 to 0.5, preferably from 0.05 to 0.5, from 0.15 to 0.5, or from 0.3 to 0.5; the alkali source (in OH)^-In terms of the first oxide) to the first oxide source (in terms of the first oxide) is from 0 to 1, preferably from 0.04 to 1, from 0.1 to 1, from 0.2 to 1, from 0.3 to 0.7 or from 0.45 to 0.7.

13. The alkylation process for preparing ethylbenzene according to any one of the preceding claims, wherein the ethylene feedstock used is one or more of pure ethylene, refinery catalytic cracking dry gas containing ethylene (preferably 10-60% by volume of ethylene), and refinery catalytic cracking dry gas containing ethylene (preferably 10-60% by volume of ethylene).

14. The alkylation process for ethylbenzene according to any of the preceding claims wherein the catalyst consists of a binder (alumina and/or silica) and the molecular sieve ((preferably the mass fraction of the molecular sieve is from 10% to 95% based on the mass of the catalyst)).

15. A process for the alkylation of ethylbenzene according to any of the preceding claims wherein the catalyst is prepared by: mixing and kneading the molecular sieve raw powder, a silicon-containing compound and/or an aluminum-containing compound, nitric acid and deionized water for molding, drying, then burning out a template agent in air at 450-550 ℃, then exchanging in an ammonium salt aqueous solution at 80-90 ℃, and finally roasting and deaminating at 500-600 ℃ for 1-5 hours to obtain a catalyst; wherein the silicon-containing compound is selected from one or more of silica sol, methyl orthosilicate and ethyl orthosilicate, and the aluminum-containing compound is selected from one or more of pseudo-boehmite, SB powder, aluminum sol and aluminum isopropoxide; the ammonium salt is selected from one or more of ammonium nitrate, ammonium chloride and ammonium sulfate.

16. The alkylation process for ethylbenzene according to any of the preceding claims wherein a mixture of a silicon containing compound and an aluminium containing compound is used in a molar ratio of from 1:1 to 1:2 based on silica to alumina.

17. A process for the alkylation of ethylbenzene according to any of the preceding claims wherein the alkylation process for ethylbenzene is carried out in a fixed bubble column reactor (preferably with both ethylene and benzene fed from the lower portion of the reactor and the reaction product withdrawn from the upper portion of the reactor), a fixed trickle bed reactor or a slurry bed reactor; and/or

The invention adopts a new molecular sieve which has the following characteristics: (1) a skeletal pore structure of extra large pores, which can be reflected at least from its higher pore volume data; (2) good thermal/hydrothermal stability and greater pore volume; as a result, the molecular sieve of the present invention is capable of adsorbing more/larger molecules, thereby exhibiting excellent adsorption/catalytic performance; (3) has unique X-ray diffraction spectrum (XRD) and unique Si/Al₂This is a molecular sieve that has not been made in the prior art; (4) has stronger acidity, especially the number of L acid centers is larger. This is a molecular sieve that has not been made in the prior art; as a result, the molecular sieve of the invention has more excellent performance particularly in acid catalysis reaction; (5) the preparation method of the molecular sieve uses an organic template agent with a specific chemical structure, thereby showing the characteristics of simple process conditions and easy synthesis of the molecular sieve product. Based on the foregoing findings, the present inventors have further found that the molecular sieve is particularly useful for catalyzing the alkylation of benzene with ethylene in the liquid phase to produce ethylbenzene, and has higher selectivityReactivity and better ethylbenzene selectivity.

Drawings

FIG. 1 is a scanning electron micrograph of the molecular sieve made in example 5.

Figure 2 is an XRD pattern of the molecular sieve made in example 5.

FIG. 3 is a scanning electron micrograph of the molecular sieve made in example 6.

Figure 4 is an XRD pattern of the molecular sieve made in example 6.

FIG. 5 is a scanning electron micrograph of the molecular sieve made in example 7.

Figure 6 is an XRD pattern of the molecular sieve made in example 7.

FIG. 7 is a scanning electron micrograph of the molecular sieve made in example 8.

Figure 8 is an XRD pattern of the molecular sieve made in example 8.

Fig. 9 is a scanning electron micrograph of the molecular sieve made in example 9.

Detailed Description

The following detailed description of the embodiments of the present invention is provided, but it should be noted that the scope of the present invention is not limited by the embodiments, but is defined by the appended claims.

All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control.

When the specification concludes with claims with the heading "known to those skilled in the art", "prior art", or the like, to derive materials, substances, methods, procedures, devices, or components, etc., it is intended that the subject matter derived from the heading encompass those conventionally used in the art at the time of filing this application, but also include those that are not currently in use, but would become known in the art to be suitable for a similar purpose.

In the context of this specification, the symbol "/" is generally understood to mean "and/or", such as the meaning of the expression "more/larger" is "more and/or larger", unless the understanding is not in line with the conventional knowledge of a person skilled in the art.

In the context of the present specification, the term organic templating agent is sometimes referred to in the art as a structure directing agent or an organic directing agent.

In the context of the present specification as C_1-4Examples of the linear or branched alkyl group include a methyl group, an ethyl group, and a propyl group.

In the context of the present invention, the term "linear or branched oxaalkylene" refers to a divalent radical obtained by interrupting the carbon chain structure of a linear or branched alkylene group by one or more (for example 1 to 3, 1 to 2 or 1) hetero groups-O-. It is preferable from the viewpoint of structural stability that, when plural, any two of the hetero groups are not directly bonded to each other. It is obvious that by interrupted it is meant that the hetero group is not at either end of the linear or branched alkylene group or the linear or branched oxaalkylene group. For example, C₄Straight chain alkylene (-CH)₂-CH₂-CH₂-CH₂-) can be interrupted by a hetero-group-O-to obtain-CH₂-O-CH₂-CH₂-CH₂-or-CH₂-CH₂-O-CH₂-CH₂-equal C₄The linear oxaheteroalkylene radical, interrupted by two hetero radicals-O-, giving-CH₂-O-CH₂-O-CH₂-CH₂-or-CH₂-O-CH₂-CH₂-O-CH₂-equal C₄Straight-chain dioxaalkylene interrupted by three hetero radicals-O-to give-CH₂-O-CH₂-O-CH₂-O-CH₂-equal C₄Straight chain trioxaalkylene. Or, specifically for example, C₄Branched alkylene (-CH)₂(CH₃)-CH₂-CH₂-) can be interrupted by a hetero-group-O-to obtain-CH₂(CH₃)-O-CH₂-CH₂-、-CH₂(CH₃)-CH₂-O-CH₂-or-CH₂(-O-CH₃)-CH₂-CH₂-equal C₄Branched mono-oxaheteroalkylene with two hetero groupsCan obtain-CH after-O-interruption₂(CH₃)-O-CH₂-O-CH₂-、-CH₂(-O-CH₃)-O-CH₂-CH₂-or-CH₂(-O-CH₃)-CH₂-O-CH₂-equal C₄Branched dioxaalkylene interrupted by three hetero radicals-O-to give-CH₂(-O-CH₃)-O-CH₂-O-CH₂-equal C₄A branched trioxalkylene group.

In the context of the present specification, the total specific surface area refers to the total area of the molecular sieve per unit mass, including the internal and external surface areas. Non-porous materials have only an external surface area, such as portland cement, some clay mineral particles, etc., while porous materials have an external surface area and an internal surface area, such as asbestos fibers, diatomaceous earth, molecular sieves, etc.

In the context of the present specification, the term pore volume, also known as pore volume, refers to the volume of pores per unit mass of a molecular sieve. The micropore volume means the volume of all micropores (i.e., pores having a pore diameter of less than 2 nm) per unit mass of the molecular sieve.

In the context of this specification, in the XRD data of molecular sieves, w, m, s, vs represent diffraction peak intensities, w is weak, m is medium, s is strong, vs is very strong, as is well known to those skilled in the art. Generally, w is less than 20; m is 20 to 40; s is 40-70; vs is greater than 70.

Unless otherwise expressly indicated, all percentages, parts, ratios, etc. mentioned in this specification are by weight unless otherwise not in accordance with the conventional knowledge of those skilled in the art.

In the context of this specification, any two or more aspects of the present invention may be combined in any combination, and the resulting solution is part of the original disclosure of this specification, and is intended to be within the scope of the present invention.

The present invention is hereby incorporated by reference in its entirety into the chinese patent application CN201710282848.1, as if fully set forth herein. The contents of the molecular sieve and the method for producing the same are described in chinese patent application CN201710282848.1, except for the following descriptions.

According to one aspect of the present invention, there is provided a molecular sieve, wherein the molecular sieve has a schematic chemical composition represented by the formula "first oxide · second oxide". It is known that molecular sieves sometimes contain some amount of moisture, particularly immediately after synthesis, but it is not considered necessary to specify this amount of moisture in the present invention because the presence or absence of this moisture does not substantially affect the XRD spectrum of the molecular sieve. In view of this, the schematic chemical composition represents, in effect, the anhydrous chemical composition of the molecular sieve. Moreover, it is apparent that the schematic chemical composition represents the framework chemical composition of the molecular sieve.

In accordance with one aspect of the present invention, the molecular sieve may further generally contain in composition, immediately after synthesis, an organic templating agent, water, and the like, such as those filling the pores thereof. Thus, the molecular sieve may sometimes have a schematic chemical composition represented by the formula "first oxide, second oxide, organic template, water". Here, the molecular sieve having the schematic chemical composition represented by the formula "first oxide/second oxide/organic template/water" can be obtained by calcining the molecular sieve having the schematic chemical composition represented by the formula "first oxide/second oxide/organic template/water" so as to remove any organic template, water, and the like present in the pore channels thereof. In addition, the calcination may be carried out in any manner conventionally known in the art, for example, the calcination temperature is generally from 300 ℃ to 750 ℃, preferably from 400 ℃ to 600 ℃, and the calcination time is generally from 1 hour to 10 hours, preferably from 3 hours to 6 hours. In addition, the calcination is generally carried out in an oxygen-containing atmosphere, such as air or oxygen.

According to an aspect of the present invention, in the foregoing schematic chemical composition, the first oxide is generally a tetravalent oxide, and for example, at least one selected from the group consisting of silicon dioxide, germanium dioxide, tin dioxide, titanium dioxide and zirconium dioxide may be mentioned, preferablySilicon dioxide (SiO)₂) Or a combination of silicon dioxide and germanium dioxide. These first oxides may be used singly or in combination in any ratio. When a plurality of kinds are used in combination, the molar ratio between any two first oxides is, for example, from 20: 200 to 35: 100. examples of the combination include a combination of silica and germanium dioxide, in which case the molar ratio of silica to germanium dioxide is, for example, from 20: 200 to 35: 100.

according to an aspect of the present invention, in the foregoing schematic chemical composition, the second oxide is generally a trivalent oxide, and for example, at least one selected from the group consisting of aluminum oxide, boron oxide, iron oxide, gallium oxide, rare earth oxide, indium oxide and vanadium oxide may be cited, and aluminum oxide (Al) is preferable₂O₃). These second oxides may be used singly or in combination in any ratio. When a plurality of kinds are used in combination, the molar ratio between any two second oxides is, for example, from 30: 200 to 60: 150.

according to an aspect of the present invention, in the foregoing schematic chemical composition, for example, any organic templating agent used in the production of the molecular sieve, and particularly, the organic templating agent used in the production of the molecular sieve according to the present embodiment, may be cited as the organic templating agent (see the detailed description below). These organic templates may be used singly or in combination in any ratio. Specifically, specific examples of the organic template include compounds represented by the following formula (I).

According to one aspect of the invention, in formula (I), the radical R₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight or branched alkylene and C_3-12A linear or branched oxaalkylene radical, the radicals R, equal to or different from each other, being independently chosen from C_1-4Straight chainOr a branched alkyl group, and X is OH.

According to one aspect of the invention, in the foregoing exemplary chemical composition, the molar ratio of the first oxide to the second oxide (e.g., SiO)₂With Al₂O₃In terms of molar ratio) is generally from 5 to ∞, preferably from 25 to 95, more preferably from 30 to 70. Here, when the molar ratio is ∞ means that the second oxide is not present or the content of the second oxide in the schematic chemical composition is negligible. The inventors of the present invention have earnestly investigated and found that the prior art has not produced, in particular, the molar ratio (e.g., SiO)₂With Al₂O₃From 25 to 95, more particularly from 30 to 70).

According to one aspect of the present invention, in the aforementioned schematic chemical composition, the molar ratio of water to the first oxide is generally from 5 to 50, preferably from 5 to 15.

According to one aspect of the present invention, in the foregoing schematic chemical composition, the molar ratio of the organic templating agent to the first oxide is generally from 0.02 to 0.5, preferably from 0.05 to 0.5, from 0.15 to 0.5, or from 0.3 to 0.5.

According to one aspect of the present invention, the molecular sieve may further contain, in its composition (typically filled in its pores), metal cations such as alkali metal and/or alkaline earth metal cations as a constituent component depending on the starting materials used in its manufacturing process. As the content of the metal cation at this time, for example, the mass ratio of the metal cation to the first oxide is generally from 0 to 0.02, preferably from 0.0002 to 0.006, but is not limited thereto in some cases.

According to one aspect of the invention, the molecular sieve has an X-ray diffraction pattern substantially as shown in the following table.

According to one aspect of the present invention, in the X-ray diffraction pattern of the molecular sieve, preferably still further comprises X-ray diffraction peaks substantially as shown in the following table.

According to one aspect of the invention, the molecular sieve has a generally columnar crystal morphology when viewed using a Scanning Electron Microscope (SEM). Here, the crystal morphology refers to the (overall) external shape that a single molecular sieve crystal exhibits in the observation field of view of the scanning electron microscope. The columnar shape is preferably a prismatic shape, particularly a hexagonal prismatic shape. Herein, the prism refers to a convex prism, and generally refers to a straight prism and a regular polygonal prism (e.g., a regular hexagonal prism). It is specifically noted that since the crystals of molecular sieves may be disturbed by various factors during growth, their actual crystal morphology may deviate to some extent, such as 30%, 20% or 5%, from the geometrical (true) right prisms or (true) regular polygonal prisms, resulting in the obtaining of tilted prisms, or irregular polygonal (even curved sided polygonal) prisms, although the present invention is not intended to specifically identify the degree of deviation. Moreover, any greater or lesser deviation may be made without departing from the scope of the invention.

According to one aspect of the invention, the molecular sieve (single crystals) generally has an effective diameter of from 100nm to 1000nm, preferably from 300nm to 700nm, when viewed using a Scanning Electron Microscope (SEM). Here, the effective diameter means that two points are arbitrarily selected along the profile (edge) of the cross section of the molecular sieve (single crystal) on the cross section, and the straight-line distance between the two points is measured, with the largest straight-line distance as the effective diameter. If the cross-sectional profile of the molecular sieve is in the form of a polygon, such as a hexagon, the effective diameter generally refers to the linear distance (diagonal distance) between the two vertices of the polygon that are farthest apart. In simple terms, the effective diameter substantially corresponds to the diameter of a circle circumscribing the polygon represented by the outline of the cross-section.

According to one aspect of the invention, the height of the molecular sieve (single crystals) is generally from 100nm to 1000nm, preferably from 150nm to 700nm, when viewed using a Scanning Electron Microscope (SEM). Here, the height refers to a straight line distance between the centers of both end faces of the pillars in a single crystal (columnar crystal) of the molecular sieve. In general, the two end faces of the molecular sieve column are substantially parallel to each other, and in this case, the linear distance is a perpendicular distance between the two end faces, but the present invention is not limited thereto.

According to one aspect of the invention, the aspect ratio of the molecular sieve (single crystals) is generally from 1/3 to 8, preferably from 1.5 to 5 or from 2 to 5, when viewed using a Scanning Electron Microscope (SEM). Here, the aspect ratio refers to a ratio of the height to the effective diameter.

According to one aspect of the invention, the total specific surface area of the molecular sieve is generally from 400m²G to 600m²G, preferably from 450m²G to 580m²(ii) in terms of/g. Here, the total specific surface area is calculated by a BET model by a liquid nitrogen adsorption method.

According to one aspect of the invention, the molecular sieve has a pore volume (micropore volume) generally of from 0.3 to 0.5ml/g, preferably from 0.30 to 0.40 ml/g. The molecular sieve of the present invention has a very high micropore volume, which indicates that it is an ultra-large pore molecular sieve. Here, the pore volume is calculated by a liquid nitrogen adsorption method according to the Horvath-Kawazoe model.

According to one aspect of the invention, the molecular sieve may be manufactured by the following manufacturing method. Here, the production method includes a step of contacting a first oxide source, a second oxide source, an optional alkali source, an organic template, and water under crystallization conditions to obtain a molecular sieve (hereinafter referred to as a contacting step).

In the method for manufacturing the molecular sieve according to an aspect of the present invention, the contacting step may be performed in any manner conventionally known in the art, such as a method of mixing the first oxide source, the second oxide source, the optional alkali source, the organic template, and water, and crystallizing the mixture under the crystallization condition.

According to an aspect of the present invention, in the contacting step, the organic template includes at least a compound represented by the following formula (I). Here, the compounds represented by the formula (I) may be used singly or in combination in any ratio.

According to one aspect of the invention, in said formula (I), the radical R₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight or branched alkylene and C_3-12Straight or branched oxaalkylene.

According to a variant embodiment of the invention, in said formula (I), the radical R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear or branched alkylene, the other being selected from C_3-12Straight or branched alkylene and C_3-12Straight or branched oxaalkylene.

According to a variant embodiment of the invention, in said formula (I), the radical R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear alkylene and the other is selected from C_4-6Linear chain of methyleneAlkyl and C_4-6A linear oxaalkylene group.

According to a variant embodiment of the invention, in said formula (I), the radical R is₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight or branched chain alkylene.

According to a variant embodiment of the invention, in said formula (I), the radical R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear alkylene and the other is selected from C_4-6A linear alkylene group.

According to a variant embodiment of the invention, in said formula (I), the radical R is₁And R₂Are different from each other, one of them is selected from C_3-12Linear or branched alkylene, the other being selected from C_3-12Straight or branched oxaalkylene.

According to an aspect of the present invention, as said C_3-12Straight-chain or branched alkylene, for example, C_3-12Specific examples of the linear alkylene group include a n-propylene group, an isopropylene group, a n-butylene group, an isobutylene group, a tert-butylene group, a n-pentylene group, an isopentylene group, a neopentylene group, a n-hexylene group, an isohexylene group, a n-octylene group, an isooctylene group, a neooctylene group, a nonylene group (or its isomer), a decylene group (or its isomer), an undecylene group (or its isomer) or a dodecylene group (or its isomer), and a n-propylene group, a n-butylene group, a n-pentylene group, a n-hexylene group, a n-heptylene group, a n-octylene group, a n-nonylene group, a n-decylene group, a n-undecylene. Further, as the above-mentioned C_3-12The straight chain alkylene group is more specifically exemplified by C_4-6Examples of the linear alkylene group include n-butylene group, n-pentylene group and n-hexylene group.

According to an aspect of the present invention, as said C_3-12Straight-chain or branched oxaalkylene, for example C_3-12The straight-chain oxaalkylene group includes, for example, - (CH)₂)₂-O-(CH₂)-、-(CH₂)₂-O-(CH₂)₂-、-(CH₂)-O-(CH₂)₃-、-(CH₂)₂-O-(CH₂)₃-、-(CH₂) -O-propylene-, - (CH)₂)-O-(CH₂)₄-、-(CH₂)-O-(CH₂)₂-O-(CH₂)-、-(CH₂)-O-(CH₂)₂-O-(CH₂)₂-、-(CH₂) -O-tert-butylidene-, - (CH)₂)₂-O-(CH₂)₄-、、-(CH₂)₃-O-(CH₂)₃-、-(CH₂) -O-neopentylene-, - (CH)₂)₂-O-(CH₂)₆-、-(CH₂)₂-O-(CH₂)₇-、-(CH₂)-O-(CH₂)₈-、-(CH₂) -O-isooctylidene-, - (CH)₂)-O-(CH₂)₁₀-、-(CH₂)₂-O-decylidene or isomers thereof-, - (CH)₂)-O-(CH₂)₆-、-(CH₂)-O-(CH₂)₇-、-(CH₂)-O-(CH₂)₈-、-(CH₂)-O-(CH₂)₁₁-、-(CH₂)-O-(CH₂)₂-O-(CH₂)-、-(CH₂)₂-O-(CH₂)₂-O-(CH₂)₂-、-(CH₂)₂-O-(CH₂)₄-O-(CH₂)₂-、-(CH₂)₂-O-(CH₂)₆-O-(CH₂)₂-or- (CH)₂)₂-O-(CH₂)₈-O-(CH₂)₂-. Further, as the above-mentioned C_3-12The linear oxaalkylene group is more specifically exemplified by C_4-6Straight-chain oxaalkylene, in particular C_4-6The straight chain monooxyheteroalkylene group may be represented by the formula- (CH)₂)_m-O-(CH₂)_m- (wherein each number m, equal to or different from each other, independently represents 2 or 3, such as 2), and more particularly- (CH)₂)₂-O-(CH₂)₂-、-(CH₂)₂-O-(CH₂)₃-、-(CH₂)₃-O-(CH₂)₃-or- (CH)₂)₂-O-(CH₂)₄-。

According to one aspect of the invention, in said formula (I), a plurality of radicals R, equal to or different from each other, are each independently selected from C_1-4The linear or branched alkyl groups are preferably each independently selected from methyl and ethyl, more preferably both methyl.

According to one aspect of the invention, in said formula (I), X is OH.

According to one aspect of the present invention, in the contacting step, the molar ratio of the organic templating agent to the first oxide source (based on the first oxide) is generally from 0.02 to 0.5, preferably from 0.05 to 0.5, from 0.15 to 0.5, or from 0.3 to 0.5.

According to an aspect of the present invention, in the contacting step, other organic templating agents conventionally used in the art for producing molecular sieves may be further used in addition to the compound represented by the formula (I) as the organic templating agent. Preferably, in the contacting step, only the compound represented by the formula (I) is used as the organic templating agent. Here, the compounds represented by the formula (I) may be used singly or in combination in any ratio.

According to an aspect of the present invention, in the contacting step, the first oxide source is generally a tetravalent oxide source, and for example, at least one selected from a silicon dioxide source, a germanium dioxide source, a tin dioxide source, a titanium dioxide source, and a zirconium dioxide source may be cited, and silicon dioxide (SiO) is preferable₂) A source or a combination of a silica source and a germanium dioxide source. These first oxide sources may be used singly or in combination of plural kinds in an arbitrary ratio. When a plurality of kinds are used in combination, the molar ratio between any two first oxide sources is, for example, from 20: 200 to 35: 100. an example of the combination includes a combination of a silica source and a germanium dioxide source, and in this case, the molar ratio of the silica source to the germanium dioxide source is determined from20: 200 to 35: 100.

according to an aspect of the present invention, in the contacting step, as the first oxide source, any corresponding oxide source conventionally used in the art for this purpose may be used, including, but not limited to, oxides, hydroxides, alkoxides, metal oxyacids, acetates, oxalates, ammonium salts, sulfates, halides, nitrates, and the like of the corresponding metal in the first oxide. For example, when the first oxide is silica, examples of the source of the first oxide include silica sol, coarse silica gel, tetraethoxysilane, water glass, white carbon, silicic acid, silica gel, potassium silicate, and the like. When the first oxide is germanium dioxide, examples of the source of the first oxide include tetraalkoxygermanium, germanium oxide, and germanium nitrate. When the first oxide is a tin dioxide source, examples of the first oxide source include tin chloride, tin sulfate, and tin nitrate. When the first oxide is titanium oxide, examples of the source of the first oxide include titanium tetraalkoxide, titanium dioxide, and titanium nitrate. When the first oxide is zirconium dioxide, examples of the source of the first oxide include zirconium sulfate, zirconium chloride, and zirconium nitrate. These first oxide sources may be used singly or in combination of plural kinds in a desired ratio.

According to an aspect of the present invention, in the contacting step, the second oxide source is generally a trivalent oxide source, and for example, at least one selected from the group consisting of an alumina source, a boron oxide source, an iron oxide source, a gallium oxide source, a rare earth oxide source, an indium oxide source, and a vanadium oxide source may be cited, and alumina (Al) is preferable₂O₃) A source. These second oxide sources may be used singly or in combination of plural kinds in an arbitrary ratio. When a plurality of species are used in combination, the molar ratio between any two second oxide sources is, for example, from 30: 200 to 60: 150.

according to an aspect of the present invention, in the contacting step, as the second oxide source, any corresponding oxide source conventionally used in the art for this purpose may be used, including but not limited to oxides, hydroxides, alkoxides, metal oxyacids, acetates, oxalates, ammonium salts, sulfates, halides, nitrates, and the like of the corresponding metal in the second oxide. For example, when the second oxide is alumina, examples of the second oxide source include aluminum chloride, aluminum sulfate, hydrated alumina, sodium metaaluminate, alumina sol, and aluminum hydroxide. When the second oxide is boron oxide, examples of the second oxide source include boric acid, borate, borax, diboron trioxide, and the like. When the second oxide is iron oxide, examples of the second oxide source include iron nitrate, iron chloride, and iron oxide. When the second oxide is gallium oxide, examples of the source of the second oxide include gallium nitrate, gallium sulfate, gallium oxide, and the like. When the second oxide is a rare earth oxide, examples of the second oxide source include lanthanum oxide, neodymium oxide, yttrium oxide, cerium oxide, lanthanum nitrate, neodymium nitrate, yttrium nitrate, and ammonium ceric sulfate. When the second oxide is indium oxide, examples of the second oxide source include indium chloride, indium nitrate, and indium oxide. When the second oxide is vanadium oxide, examples of the second oxide source include vanadium chloride, ammonium metavanadate, sodium vanadate, vanadium dioxide, vanadyl sulfate, and the like. These second oxide sources may be used singly or in combination of plural kinds in a desired ratio.

According to an aspect of the invention, in the contacting step, the first oxide source (based on the first oxide, such as SiO) is provided₂) With said second oxide source (based on said second oxide, such as Al)₂O₃) The molar ratio of (a) is generally from 5 to ∞, preferably from 25 to 95, more preferably from 30 to 70. Here, when the molar ratio is ∞ means that the second oxide source is not used or is not intentionally introduced into the contacting step.

According to one aspect of the invention, in the contacting step, the molar ratio of water to the first oxide source (based on the first oxide) is generally from 5 to 50, preferably from 5 to 15.

According to an aspect of the present invention, in the contacting step, an alkali source may or may not be used. The group X contained in the compound represented by the formula (I) can be used to provide the OH group required therein without the intentional use of an alkali source^-. Here, as the alkali source, any alkali source conventionally used in the art for this purpose may be used, including but not limited to inorganic bases having an alkali metal or an alkaline earth metal as a cation, particularly sodium hydroxide, potassium hydroxide and the like. These alkali sources may be used singly or in combination of two or more in an arbitrary ratio.

According to one aspect of the invention, in the contacting step, the source of alkalinity (in OH)^-In terms of the first oxide) to the first oxide source (in terms of the first oxide) is generally from 0 to 1, preferably from 0.04 to 1, from 0.1 to 1, from 0.2 to 1, from 0.3 to 0.7 or from 0.45 to 0.7.

According to an aspect of the present invention, in the contacting step, as the crystallization condition, the crystallization temperature is generally from 80 ℃ to 120 ℃, preferably from 120 ℃ to 170 ℃ or from 120 ℃ to 200 ℃.

According to an aspect of the present invention, in the contacting step, as the crystallization condition, the crystallization time is generally at least 1 day, preferably at least 2 days, preferably from 3 days to 8 days, from 5 days to 8 days, or from 4 days to 6 days.

According to an aspect of the present invention, in the method for producing a molecular sieve, after the contacting step is completed, the molecular sieve may be separated from the obtained reaction mixture as a product by any separation means conventionally known. Herein, the molecular sieve product comprises the molecular sieve of the present invention. In addition, as the separation method, for example, a method of filtering, washing and drying the obtained reaction mixture may be mentioned.

According to an aspect of the present invention, in the method for manufacturing the molecular sieve, the filtering, washing and drying may be performed in any manner conventionally known in the art. Specifically, for example, the reaction mixture obtained may be simply filtered by suction. As the washing, for example, washing with deionized water until the filtrate has a pH of 7 to 9, preferably 8 to 9, can be mentioned. The drying temperature is, for example, 40 to 250 ℃ and preferably 60 to 150 ℃, and the drying time is, for example, 8 to 30 hours and preferably 10 to 20 hours. The drying may be carried out under normal pressure or under reduced pressure.

According to an aspect of the present invention, the method for producing the molecular sieve may further include a step of subjecting the obtained molecular sieve to calcination (hereinafter, referred to as calcination step) as necessary to remove the organic template and moisture and the like that may be present, thereby obtaining a calcined molecular sieve. In the context of the present specification, the molecular sieves before and after calcination are also collectively referred to as the molecular sieve of the invention or the molecular sieve according to the invention.

According to one aspect of the present invention, in the method for manufacturing a molecular sieve, the calcination may be carried out in any manner conventionally known in the art, such as calcination temperature is generally from 300 ℃ to 750 ℃, preferably from 400 ℃ to 600 ℃, and calcination time is generally from 1 hour to 10 hours, preferably from 3 hours to 6 hours. In addition, the calcination is generally carried out in an oxygen-containing atmosphere, such as air or oxygen.

According to one aspect of the present invention, the molecular sieve of the present invention or any molecular sieve produced by the method for producing a molecular sieve according to the present invention (in the context of the present specification, both are also collectively referred to as the molecular sieve of the present invention or the molecular sieve according to the present invention), may also be subjected to ion exchange by any means conventionally known in the art, as needed, such as by replacing all or part of the metal cations (such as Na ions or K ions, depending on the specific method for producing them) contained in its composition with other cations by an ion exchange method or a solution impregnation method (see, for example, U.S. Pat. nos. 3140249 and 3140253, etc.). Examples of the other cation include a hydrogen ion, other alkali metal ion (including K ion, Rb ion, etc.), and ammonium ion (including NH)₄Ionic, quaternary ammonium ions such as tetramethylAmmonium ion, tetraethylammonium ion, and the like), alkaline earth metal ion (including Mg ion, Ca ion), Mn ion, Zn ion, Cd ion, noble metal ion (including Pt ion, Pd ion, Rh ion, and the like), Ni ion, Co ion, Ti ion, Sn ion, Fe ion, and/or rare earth metal ion, and the like.

The molecular sieve according to the present invention may be further treated with a dilute acid solution or the like as necessary to increase the silica-alumina ratio, or treated with water vapor to increase the acid-erosion resistance of the molecular sieve crystals.

The molecular sieve according to the invention has good thermal/hydrothermal stability and has larger pore volume. As a result, the molecular sieve of the present invention is capable of adsorbing more/larger molecules, thereby exhibiting excellent adsorption/catalytic performance.

The molecular sieve according to the invention has a strong acidity, in particular a high number of L acid centers. This is a molecular sieve that has not been produced in the prior art. As a result, the molecular sieves of the present invention have superior performance characteristics, particularly in acid catalyzed reactions.

The molecular sieve according to the invention may be in any physical form, such as a powder, granules or molded article (e.g. a strip, a trilobe, etc.). These physical forms can be obtained in any manner conventionally known in the art and are not particularly limited.

The molecular sieve according to the invention may be used in combination with other materials, thereby obtaining a molecular sieve composition. Examples of the other materials include active materials and inactive materials. Examples of the active material include synthetic zeolite and natural zeolite, and examples of the inactive material (generally referred to as a binder) include clay, silica gel, and alumina. These other materials may be used singly or in combination in any ratio. As the amount of the other materials, those conventionally used in the art can be directly referred to, and there is no particular limitation.

According to the alkylation method of the present invention, the silica-alumina ratio of the molecular sieve is preferably 30 to 150, and more preferably 40 to 120, based on the molar ratio of silica to alumina.

According to the alkylation process of the present invention, the catalyst preferably consists of the aforementioned molecular sieve and the balance binder. The mass fraction of the catalyst is 15 to 95%, preferably 40 to 80%, based on the mass of the catalyst.

According to the alkylation process of the present invention, the binder is preferably silica and/or alumina.

According to the alkylation process of the present invention, a suitable catalyst is prepared by: mixing, kneading and extruding the molecular sieve raw powder, a precursor (a silicon compound and/or an aluminum compound) of a binder, nitric acid and deionized water into strips, drying, roasting in air at about 550 ℃, removing a template agent, exchanging for 1-2 times with an ammonium salt aqueous solution at 70-90 ℃, washing, drying, and roasting at 500-600 ℃ for deamination for 1-5 hours to obtain the catalyst.

Another suitable catalyst preparation for the alkylation process according to the invention is: roasting the molecular sieve raw powder in air at about 550 ℃, removing a template agent, exchanging for 1-2 times by using an ammonium salt aqueous solution at 70-90 ℃, then washing, drying, roasting and deaminating for 1-5 hours at 500-600 ℃, kneading and extruding the mixture with a precursor (silicon compound and/or aluminum compound) of a binder, nitric acid and deionized water to form strips, drying, and roasting for 1-5 hours at 450-550 ℃ to obtain the catalyst.

According to the alkylation method, the precursor of the binder can be a silicon-containing compound and/or an aluminum-containing compound, wherein the silicon-containing compound can be one or more selected from silica sol, methyl orthosilicate and ethyl orthosilicate; the aluminium-containing compound may be selected from one or more of pseudo-boehmite, SB powder, alumina sol and aluminium isopropoxide. When a mixture of a silicon-containing compound and an aluminum-containing compound is used, the mass ratio of the mixture of the silicon-containing compound and the aluminum-containing compound to the aforementioned molecular sieve is 10:95 to 40:60, preferably 15:85 to 30:70, based on the total mass of silicon oxide and aluminum oxide; wherein the ratio of the silicon-containing compound to the aluminum-containing compound is 1:1 to 1:2 in terms of the molar ratio of silicon oxide to aluminum oxide.

According to the alkylation method of the invention, the ethylene raw material is one or more of pure ethylene, refinery catalytic cracking dry gas containing ethylene (preferably the volume fraction of the ethylene is 10-60%) and refinery catalytic cracking dry gas containing ethylene (preferably the volume fraction of the ethylene is 10-60%). Catalytic Cracking (FCC) and catalytic cracking are important petroleum processing processes, and waste tail gases (FCC dry gas, catalytic cracking dry gas and the like) generated by the processing processes are collectively called catalytic dry gas. The catalytic dry gas contains a small amount of C in addition to ethylene₃H₆，H₂，CH₄，C₂H₆，C₃H₈，CO,CO₂，H₂O,H₂S and the like. The dry gas must be refined to remove acid gases including hydrogen sulfide and carbonyl sulfide, alkali nitrogen including ammonia and other basic nitrogen compounds, and water before entering the reactor.

According to the alkylation process of the present invention, the alkylation reaction conditions may be: the temperature is 140-280 ℃, preferably 160-250 ℃; the reaction pressure is 1MPa to 4MPa, preferably 1.2Pa to 3.6 MPa; the molar ratio of benzene to ethylene in the feed is 1: 1-12: 1, and the preferable ratio of benzene to ethylene is 4: 1-12: 1; the weight hourly space velocity measured by ethylene is 0.1h^-1～0.8h^-1Preferably 0.1h^-1～0.5h^-1。

According to the alkylation process of the present invention, the reactor in which the alkylation reaction is carried out may be, but is not limited to, a fixed bubble bed reactor, a fixed trickle bed reactor or a slurry bed reactor, preferably a fixed bubble bed reactor. When a fixed bubble bed reactor is used, both ethylene and benzene are fed from the lower end of the reactor and the reaction product is drawn from the upper part. In the case of a fixed trickle bed reactor, ethylene is fed from the bottom of the reactor, benzene is fed from the middle or upper part of the reactor, and the reaction product is withdrawn from the bottom of the reactor.

The present invention will be described in further detail with reference to examples, but the present invention is not limited to these examples.

In the context of the present specification, including in the examples and comparative examples below, XRD testing was performed using a Netherland, PANALYTICAL Corporation apparatus. And (3) testing conditions are as follows: cu target, Ka radiation, Ni filter, tube voltage of 40kV, tube current of 40mA, and scanning range of 2-50 deg.

In the context of the present specification, including the following examples and comparative examples, a scanning electron microscope of Quanta 200F (20kv) model of FEI company, usa was used. And (3) testing conditions are as follows: a suspension method is adopted for sample preparation, and 0.01g of molecular sieve sample is put into a 2mL glass bottle. Dispersing with anhydrous ethanol, shaking, dropping with a dropper onto a sample net with diameter of 3mm, drying, placing in a sample injector, and observing with an electron microscope. The observation may use a magnification of 1 ten thousand times or a magnification of 5 ten thousand times. In addition, the molecular sieve is observed under the magnification of 5 ten thousand times, an observation field is randomly selected, and the average value of the sum of the effective diameters and the average value of the sum of the heights of all the molecular sieve crystals in the observation field are calculated. This operation was repeated a total of 10 times. The effective diameter and height were determined as the average of the sum of the average values of 10 times.

In the context of the present specification, including the examples and comparative examples below, the U.S. Varian is used^UNITYINOVA 500MHz NMR spectrometer. And (3) testing conditions are as follows: using a solid dual-resonance probe, 4mm phi ZrO₂And a rotor. Experimental parameters: the test temperature is room temperature, the number of scanning times nt is 5000, the pulse width pw is 3.9 mus, the spectrum width sw is 31300Hz, the resonance frequency Sfrq of the observed nucleus is 125.64MHz, the sampling time at is 0.5s, and the chemical shift calibration delta _TMS0, delay time d1 is 4.0s, decoupling mode dm is nny (anti-gated decoupling), deuterated chloroform lock field.

In the context of the present specification, including the following examples and comparative examples, an X-ray fluorescence spectrometer model 3013, manufactured by japan food electronics corporation, was used. And (3) testing conditions are as follows: tungsten target, excitation voltage 40kV, excitation current 50 mA. The experimental process comprises the following steps: the sample is pressed into a sheet and then arranged on an X-ray fluorescence spectrometer, and the sample emits fluorescence under the irradiation of X-rays, wherein the following relationship exists between the fluorescence wavelength lambda and the atomic number Z of the element: k (Z-S)^-2K is a constant, and as long as the wavelength λ of fluorescence is measured, the element can be identified. Measuring characteristic spectral line of each element by using scintillation counter and proportional counterThe intensity of (c) is analyzed quantitatively or semi-quantitatively.

In the context of this specification, including the examples and comparative examples below, all medicaments and starting materials are either commercially available or can be manufactured according to established knowledge.

In the context of the present specification, including in the examples and comparative examples below, the total specific surface area, pore volume and pore diameter of the molecular sieve were measured according to the following analytical methods.

Equipment: micromeritic ASAP2010 static nitrogen adsorption instrument

Measurement conditions were as follows: the sample was placed in a sample handling system and evacuated to 1.33X 10 at 350 deg.C^-2Pa, keeping the temperature and the pressure for 15h, and purifying the sample. And measuring the adsorption quantity and the desorption quantity of the purified sample on nitrogen under different specific pressures of P/P0 at the liquid nitrogen temperature of-196 ℃ to obtain an adsorption-desorption isothermal curve. Then, the total specific surface area is calculated by utilizing a two-parameter BET formula, the adsorption capacity below a specific pressure P/P0 which is approximately equal to 0.98 is taken as the pore volume of the sample, and the pore size distribution is calculated by using a BJH model.

In the context of the present specification, including the examples and comparative examples below, dilute ethylene is formulated with pure ethylene and nitrogen, the volume fraction of ethylene being 15%.

In the context of this specification, including the examples and comparative examples below, a process for the dilute ethylene liquid phase process for making ethylbenzene is carried out using a bubbling bed reactor. The reactor is a stainless steel tube type isothermal reaction tube, the inner diameter is 12mm, the catalyst loading is 8mL, and benzene and ethylene (including dilute ethylene) are introduced from the bottom of the reaction tube.

The ethylene conversion and ethylbenzene selectivity are calculated by the following equations:

ethylene conversion XE ═ mole of ethylene in the feed-mole of ethylene in the liquid discharge-mole of ethylene in the gas discharge)/mole of ethylene in the feed x 100%

Ethylbenzene selectivity SEB ═ mole fraction of ethylbenzene/(mole fraction of 1-benzene) × 100%

Example 1

Preparation of templating agent a 1:

15g (0.0)87mol) of tetramethylhexanediamine is added into a 500ml three-necked bottle, 250ml of isopropanol is added, 18.8g (0.087mol) of 1, 4-dibromobutane is dropwise added at room temperature, after 15min, the dropwise addition is finished, the temperature is raised to reflux, the solution gradually becomes white turbid from colorless and transparent, High Performance Liquid Chromatography (HPLC) is used for tracking the complete reaction of raw materials, 200ml of ethyl acetate is added into the reaction solution after the reaction is carried out for 1h, the reflux is carried out, the filtration is carried out after the cooling, the obtained solid is sequentially washed by ethyl acetate and ether, 30g of white solid product, namely 1,1,6, 6-tetramethyl-1, 6-diaza-dodecacyclo-1, 6-dibromo salt, the relative molecular weight is 388.2, the melting point is 273.7 ℃,¹chemical shifts of HNMR spectrum (300MHz, CDCl)₃) δ (ppm) is: 1.50(t,4H),1.90(t,8H),3.14(s,12H),3.40(t, 8H).

Preparation of templating agent B1: replacing Br in the template agent A1 with OH by adopting an ion exchange method; the ion exchange resin is strong-base styrene anion exchange resin, the working solution is a 15 m% template agent A1 aqueous solution, the operating temperature is 25 ℃, and the mass ratio of the working solution to the ion exchange resin is 1: 3; the flow rate was 3 drops/second; and (3) removing water from the exchanged solution by using a rotary evaporator to obtain the product, wherein the relative molecular weight of the product is 262.2, the purity of the product is 99.21 percent, and the bromine content of the product is 0.79m percent.

Example 2

Preparation of template C1

Adding 10g (0.058mol) of tetramethylhexanediamine into a 500ml three-necked bottle, adding 250ml of isopropanol, dropwise adding 16.6g (0.058mol) of 1, 9-dibromononane at room temperature, after 15min, heating to reflux, gradually changing the solution from colorless transparency to white turbidity, tracking the reaction of the raw materials by High Performance Liquid Chromatography (HPLC), adding 200ml of ethyl acetate into the reaction solution after the reaction is completed, refluxing for 1h, cooling, performing suction filtration, washing the obtained solid with ethyl acetate and diethyl ether in sequence to obtain 25g of a white solid product, namely 1,1,8, 8-tetramethyl-1, 8-diaza heptadecyl-1, 8-dibromo salt, with the relative molecular weight of 458.4, and the white solid product has the molecular weight of 458.4¹Chemical shifts of HNMR spectrum (300MHz, CDCl)₃) δ (ppm) is: 1.51(t,14H),1.92(t,8H),3.16(s,12H),3.40(t, 8H).

Preparation of templating agent D1: replacing Br in the template agent C1 with OH by adopting an ion exchange method; the ion exchange resin is strong-base styrene anion exchange resin, the working solution is a 15 m% template agent C1 aqueous solution, the operating temperature is 25 ℃, and the mass ratio of the working solution to the ion exchange resin is 1: 3; the flow rate was 3 drops/second; and (3) removing water from the exchanged solution by using a rotary evaporator to obtain the product, wherein the relative molecular weight of the product is 332.4, the purity of the product is 99.8 percent, and the bromine content of the product is 0.2m percent.

Example 3

Preparation of templating agent a 2: 15g (0.094mol) of bis [2- (N, N-dimethylaminoethyl)]Adding ether into a two-neck flask, adding 100mL of isopropanol, dropwise adding 9.5g (0.047mol) of 1, 3-dibromopropane under stirring at 25 ℃, heating to reflux temperature after dropwise adding, refluxing for 30min to change the solution from colorless to white turbid, reacting for 12h at the reflux temperature, cooling to 25 ℃, adding 50mL of ethyl acetate, stirring for 15min to form white turbid liquid, filtering, and washing the obtained solid with ethyl acetate to obtain 13.2g of a product. Its melting point is 250.3 deg.C, purity is 99.9 m%, relative molecular weight is 362.2, chemical shift of 1H-NMR spectrum (300MHZ, internal standard TMS, solvent CDCl)₂) δ (ppm) is: 1.49(2H, m),2.27(4H, m),2.36(4H, t),2.53(4H, t),3.47(4H, t).

Preparation of templating agent B2: replacing Br in the template agent A2 with OH by adopting an ion exchange method; the ion exchange resin is strong-base styrene anion exchange resin, the working solution is a 15 m% template agent A2 aqueous solution, the operating temperature is 25 ℃, and the mass ratio of the working solution to the ion exchange resin is 1: 3; the flow rate was 3 drops/second; and (3) removing water from the exchanged solution by using a rotary evaporator to obtain the product, wherein the relative molecular weight is 236.2, the purity is 98.2m percent, and the bromine content is 0.79m percent.

Example 4

Preparation of templating agent C2: the preparation was carried out as template A2 in example 3, except that 12.78g (0.047mol) of 1, 8-dibromooctane were used instead of 1, 3-dibromopropane. The test gave 17.6g of product having a melting point of 288.2 ℃, a relative molecular weight of 432.2 and a purity of 99.9 m%, and chemical shifts of the 1H-NMR spectrum (300MHZ, internal standard TMS, solvent CDCl)₂) δ (ppm) is: 1.29(2H, s),1.39(2H, m),1.43(2H, s), 2.27(2H, m),2.36 (2H, m), 2.55(2H, m), 3.63(4H, m).

Preparation of templating agent D2: replacing Br in the template agent C2 with OH by adopting an ion exchange method; the ion exchange resin is strong-base styrene anion exchange resin, the working solution is a 15 m% template agent C2 aqueous solution, the operating temperature is 25 ℃, and the mass ratio of the working solution to the ion exchange resin is 1: 3; the flow rate was 3 drops/second; and (3) removing water from the exchanged solution by using a rotary evaporator to obtain the product, wherein the relative molecular weight of the compound is 306.2, the purity of the compound is 99.5m percent, and the bromine content of the compound is 0.2m percent.

Example 5

1.23g of sodium metaaluminate is charged into a 45mL Teflon container, 1.925g of template B2 is added, and 9g of silica sol (Qingdao ocean chemical Co., Ltd., Industrial product, SiO) is added₂The content is 30%), standing and aging are carried out for 1h, and the components are fully mixed according to the molar ratio: SiO 2₂/Al₂O₃＝35、H₂O/SiO₂7.1, template B2/SiO₂＝0.15,NaOH/SiO₂0.12. The above mixture was charged into a 45mL steel autoclave with a Teflon liner, which was covered and sealed, and the autoclave was placed in a rotary convection oven set at 20rpm, reacted at 120 ℃ for 1 day and then heated to 150 ℃ for 5 days. Taking out the autoclave and rapidly cooling the autoclave to room temperature, separating the mixture on a high-speed centrifuge with 5000rpm, collecting the solid, fully washing the solid with deionized water, and drying the solid for 5 hours at 100 ℃ to obtain the product.

The scanning electron micrograph of the product is shown in figure 1, which obviously shows that the molecular sieve has a hexagonal prism-shaped crystal morphology, the effective diameter is 1200nm, the height is 1000nm, and the height-diameter ratio is 0.833. The total specific surface area of the molecular sieve is measured to be 558m²The pore volume was 0.51 ml/g. The XRD pattern of the product is shown in FIG. 2. The silicon to aluminum ratio of the product was 36.38.

Example 6

Adding 0.134g of sodium metaaluminate into a 45mL Teflon container, adding 1.81g of template agent B1, stirring for 30 minutes until uniform, and adding 3g of coarse silica gel (Qingdao ocean chemical Co., Ltd., Industrial product, SiO)₂Content 98.05%) and 6.3g of deionized water, stirring for 5 minutes and fully mixing, wherein the molar ratio of each component is as follows: SiO 2₂/Al₂O₃＝25、H₂O/SiO₂7, template B1/SiO₂＝0.16、OH^-/SiO₂＝0.31。

The above mixture was charged into a 45mL steel autoclave with a Teflon liner, which was covered and sealed, and the autoclave was placed in a rotary convection oven at a rotation speed set at 20rpm and reacted at 150 ℃ for 5 days. Taking out the autoclave and rapidly cooling the autoclave to room temperature, separating the mixture on a high-speed centrifuge with 5000rpm, collecting the solid, fully washing the solid with deionized water, and drying the solid for 5 hours at 100 ℃ to obtain the product.

The scanning electron micrograph of the product is shown in FIG. 3, and it is obvious that the molecular sieve has a hexagonal prism-shaped crystal morphology. The total specific surface area of the molecular sieve is measured to be 523m²The pore volume is 0.356 ml/g. XRF analysis results showed Si/Al₂23. The XRD pattern of the product is shown in FIG. 4.

Example 7

6.975g of template agent D1 was added to a 45mL Teflon container, 0.296g of sodium metaaluminate was added, the mixture was stirred for 30 minutes until uniform, and then 3g of coarse silica gel (Qingdao ocean chemical Co., Ltd., Industrial product, SiO) was added₂98% of Al₂O₃Content 0.253%). Standing and aging for 1h, and fully mixing, wherein the molar ratio of each component is as follows: SiO 2₂/Al₂O₃＝201，H₂O/SiO₂5.8, template D1/SiO₂＝0.15，NaOH/SiO₂＝0.05。

The above mixture was charged into a 45mL steel autoclave with a Teflon liner, which was covered and sealed, and the autoclave was placed in a rotary convection oven set at 20rpm, reacted at 120 ℃ for 1 day, and then heated to 160 ℃ for 5 days. Taking out the autoclave and rapidly cooling the autoclave to room temperature, separating the mixture on a high-speed centrifuge with 5000rpm, collecting the solid, fully washing the solid with deionized water, and drying the solid for 5 hours at 100 ℃ to obtain the product.

The scanning electron micrograph of the product is shown in FIG. 5, and it is obvious that the molecular sieve has a hexagonal prism-shaped crystal morphology. The total specific surface area of the molecular sieve is measured to be 564m²The pore volume is 0.394 ml/g. The XRD pattern of the product is shown in FIG. 6. XRF analysis results show molecular sieve Si/Al₂＝203。

Example 8

0.735g of sodium metaaluminate is charged into a 45mL Teflon container, 8.024g of template B2 is added, and then 3g of coarse silica gel (Qingdao ocean chemical Co., Ltd., Industrial, SiO)₂The content is 98.05 percent), standing and aging for 1 hour, and fully mixing, wherein the molar ratio of each component is as follows: SiO 2₂/Al₂O₃＝80、H₂O/SiO₂7.5, template B2/SiO₂0.15. The above mixture was charged into a 45mL steel autoclave with a Teflon liner, which was covered and sealed, and the autoclave was placed in a rotary convection oven set at 20rpm, reacted at 120 ℃ for 1 day and then heated to 150 ℃ for 5 days. Taking out the autoclave and rapidly cooling the autoclave to room temperature, separating the mixture on a high-speed centrifuge with 5000rpm, collecting the solid, fully washing the solid with deionized water, and drying the solid for 5 hours at 100 ℃ to obtain the product.

The scanning electron micrograph of the product is shown in figure 7, and the molecular sieve is obviously seen to have the flat prism-shaped or flat cylindrical crystal morphology. The total specific surface area of the molecular sieve was measured to be 482m²The pore volume is 0.346 ml/g. XRF analysis results showed Si/Al₂84. The XRD pattern of the product is shown in FIG. 8.

Example 9

0.132g of sodium metaaluminate is charged into a 45mL Teflon container, 8.731g of template D2 is added, and then 3g of coarse silica gel (Qingdao ocean chemical Co., Ltd., Industrial product, SiO) is added₂The content is 98.05 percent), standing and aging for 1 hour, and fully mixing, wherein the molar ratio of each component is as follows: SiO 2₂/Al₂O₃＝60、H₂O/SiO ₂8, template agent D2/SiO₂0.15. The above mixture was charged into a 45mL steel autoclave with a Teflon liner, which was covered and sealed, and the autoclave was placed in a rotary convection oven set at 20rpm, reacted at 120 ℃ for 1 day, and then heated to 150 ℃ for 4 days. Taking out the autoclave and rapidly cooling to room temperature, separating the mixture in a high speed centrifuge at 5000rpm, collecting the solid, washing thoroughly with deionized water, drying at 100 deg.C for 5 hrAnd (5) obtaining the product after aging.

The scanning electron micrograph of the product is shown in FIG. 9, and it is obvious that the molecular sieve has flat prism or flat cylindrical crystal morphology. The total specific surface area of the molecular sieve was measured to be 452m²The pore volume is 0.385 ml/g. XRF analysis results showed Si/Al₂＝62。

Example 10

Molecular sieves were prepared according to the method of example 5, except that the amount of silica sol was 10g, and the final product Si/Al₂＝42。

Example 11

88g of the molecular sieve raw powder prepared in example 10 (the silica-alumina ratio is 42, the ignition weight loss is 15%) and 31.25g of pseudo-boehmite (the mass fraction of alumina is 80%) are uniformly mixed, a proper amount of nitric acid and deionized water are added, the mixture is kneaded, extruded, formed, dried, heated to 540 ℃ by a program, roasted for 5 hours, then ammonia exchange is carried out for 2 times at 80 ℃ by using 0.5mol/L ammonium nitrate solution, each time lasts for 2 hours, and then the catalyst A is prepared by washing, drying for 12 hours at 90 ℃ and roasting for 3 hours at 550 ℃.

On a bubbling bed reaction evaluation device, a 20-40-mesh catalyst A is adopted to catalyze the ethylbenzene reaction by a dilute ethylene liquid phase method, the concentration of dilute ethylene is 15%, and the device is prepared by adopting pure ethylene and nitrogen. The catalyst loading is 2g, the benzene-olefin ratio is 12, the reaction temperature is 200 ℃, the reaction pressure is 3.5MPa, and the weight hourly space velocity of ethylene is 0.32h^-1。

The reaction results are shown in Table 1.

Example 12

A catalyst was prepared as in example 11, except that: the molecular sieve used was made as in example 8. Thus obtaining the catalyst B.

The process of example 11 was used to carry out the dilute ethylene liquid phase process ethylbenzene reaction with the only differences being: using catalyst B, the reaction temperature is 250 ℃, and the weight hourly space velocity of ethylene is 0.15h^-1。

The reaction results are shown in Table 1.

Example 13

A catalyst was prepared as in example 11, except that: the molecular sieve used was made as in example 9. Thus obtaining catalyst C.

The alkylation reaction conditions of example 11 were used to carry out the reaction of ethylbenzene in the liquid phase production of pure ethylene, except that catalyst C was used, the reaction temperature was 150 ℃, the reaction pressure was 1.5MPa, and the weight hourly space velocity of ethylene was 0.3h^-1。

The reaction results are shown in Table 1.

Example 14

100g of the molecular sieve raw powder prepared in the example 10 (the silica-alumina ratio is 42, and the ignition weight loss is 15%) is heated to 540 ℃ by a program, and is roasted for 5 hours, then 0.5mol/L ammonium nitrate solution is used for ammonia exchange for 2 times at 80 ℃, and each time is 2 hours, and then the molecular sieve is washed by water, dried at 90 ℃ for 12 hours, and roasted at 550 ℃ for 3 hours to prepare a hydrogen type molecular sieve; 60g of hydrogen type molecular sieve, 66.67g of silica sol (the mass fraction of silicon dioxide is 30%) and 66.67g of alumina sol (the mass fraction of aluminum oxide is 30%) are uniformly mixed, a proper amount of nitric acid and deionized water are added, and after kneading, extruding, molding and drying, the temperature is programmed to 540 ℃, and the catalyst D is prepared by roasting for 3 hours.

On a bubbling bed reaction evaluation device, a 20-40-mesh catalyst D is adopted to catalyze the reaction of pure ethylene and benzene by a liquid-phase method for preparing ethylbenzene, the catalyst loading is 2g, the benzene-olefin ratio is 12, the reaction temperature is 200 ℃, the reaction pressure is 3.5MPa, and the weight hourly space velocity of ethylene is 0.32h^-1。

The reaction results are shown in Table 1.

Example 15

Catalyst D prepared in example 14 was used.

The alkylation reaction conditions of example 14 were used to carry out the reaction for preparing ethylbenzene by a pure ethylene liquid phase process, except that the reaction temperature was 250 ℃, the benzene-to-olefin ratio was 6, and the weight hourly space velocity of ethylene was 0.32h^-1。

The reaction results are shown in Table 1.

Example 16

Catalyst a prepared in example 11 was used.

The alkylation reaction conditions of example 14 were used to carry out the reaction of ethylbenzene in the liquid phase production of pure ethylene, except that catalyst a was used, the reaction temperature was 180 ℃, the benzene-to-olefin ratio was 9, and the reaction pressure was 2.0MPa and the weight hourly space velocity of ethylene is 0.50h^-1。

The reaction results are shown in Table 1.

TABLE 1

As can be seen from Table 1, the method for preparing ethylbenzene by alkylating ethylene and benzene provided by the invention has higher ethylene conversion rate and good ethylbenzene selectivity.

Although the embodiments of the present invention have been described in detail with reference to the embodiments and the drawings, it should be noted that the scope of the present invention is not limited by the embodiments, but is defined by the claims. Those skilled in the art can appropriately modify the embodiments without departing from the technical spirit and scope of the present invention, and the modified embodiments are also clearly included in the scope of the present invention.

Claims

1. A process for the liquid phase alkylation of benzene with ethylene to produce ethylbenzene comprising the catalytic reaction of ethylene and benzene under alkylation reaction conditions in the presence of a catalyst, wherein the catalyst comprises a molecular sieve having a chemical composition represented by the formula "first oxide-second oxide" or "first oxide-second oxide-organic templating agent-water", wherein the molar ratio of said first oxide to said second oxide is from 5 to ∞; the first oxide is selected from at least one of silicon dioxide, germanium dioxide, tin dioxide, titanium dioxide and zirconium dioxide, and the second oxide is selected from at least one of aluminum oxide, boron oxide, iron oxide, gallium oxide, rare earth oxide, indium oxide and vanadium oxide; the molar ratio of water to the first oxide is from 5 to 50; a molar ratio of the organic templating agent to the first oxide is from 0.02 to 0.5, and has an X-ray diffraction pattern substantially as shown in the following Table,

2. the process of claim 1 wherein the molar ratio of said first oxide to said second oxide is from 30 to 150.

3. The process of claim 2 wherein the molar ratio of said first oxide to said second oxide is from 40 to 120.

4. The method of claim 1 wherein the first oxide is silicon dioxide or a combination of silicon dioxide and germanium dioxide.

5. The method of claim 1, wherein the second oxide is alumina.

6. The process of claim 1 wherein the molar ratio of water to said first oxide is from 5 to 15.

7. The process of claim 1 wherein the molar ratio of said organic templating agent to said first oxide is from 0.05 to 0.5.

8. The method of claim 7 wherein the molar ratio of said organic templating agent to said first oxide is from 0.15 to 0.5.

9. The method of claim 8 wherein the molar ratio of said organic templating agent to said first oxide is from 0.3 to 0.5.

10. The method of claim 1, wherein the ethylene feedstock used is one or more of pure ethylene, refinery catalytically cracked dry gas containing ethylene, and refinery catalytically cracked dry gas containing ethylene.

11. The method according to claim 10, wherein the ethylene-containing refinery catalytic cracking dry gas has an ethylene volume fraction of 10% to 60%.

12. The method of claim 10, wherein the ethylene-containing refinery catalytically cracked dry gas has an ethylene volume fraction of 10% to 60%.

13. The process of claim 1 wherein the catalyst is comprised of a binder and the molecular sieve is present in a mass fraction of 15 to 95% based on the mass of the catalyst.

14. The method of claim 13, wherein the binder is alumina and/or silica.

15. The process of claim 13 wherein the catalyst is prepared by: mixing and kneading the molecular sieve raw powder, a silicon-containing compound and/or an aluminum-containing compound, nitric acid and deionized water for molding, drying, then burning out a template agent in air at 450-550 ℃, then exchanging in an ammonium salt aqueous solution at 80-90 ℃, and finally roasting and deaminating at 500-600 ℃ for 1-5 hours to obtain a catalyst; wherein the silicon-containing compound is selected from one or more of silica sol, methyl orthosilicate and ethyl orthosilicate, and the aluminum-containing compound is selected from one or more of pseudo-boehmite, SB powder, aluminum sol and aluminum isopropoxide; the ammonium salt is selected from one or more of ammonium nitrate, ammonium chloride and ammonium sulfate.

16. The process according to claim 15, wherein a mixture of a silicon-containing compound and an aluminum-containing compound is used in a molar ratio of 1:1 to 1:2, based on silicon oxide and aluminum oxide.

17. The process according to claim 1, characterized in that the process is carried out in a fixed bubble bed reactor, a fixed trickle bed reactor or a slurry bed reactor.

18. The process of claim 1 wherein the alkylation reaction conditions are: the reaction temperature is 150-280 ℃, the reaction pressure is 1-4 MPa, and the molar ratio of benzene to ethylene is 1: 1-15: 1, weight hourly space velocity in terms of ethylene of 0.1h^-1～0.8h^-1。

19. The process of claim 1 wherein the alkylation reaction conditions are: the reaction temperature is 160-250 ℃, the reaction pressure is 1.2-3.6 MPa, and the molar ratio of benzene to ethylene is 3: 1-12: 1, weight hourly space velocity in terms of ethylene of 0.1h^-1～0.5h^-1。

20. A process for the liquid phase alkylation of benzene with ethylene to produce ethylbenzene comprising the step of contacting ethylene and benzene under alkylation reaction conditions in the presence of a catalyst, wherein the catalyst comprises a molecular sieve produced by the process comprising: contacting under crystallization conditions a first source of oxide, a second source of oxide, optionally a source of base, an organic templating agent, and water to obtain said molecular sieve; wherein, optionally, a step of calcining the obtained molecular sieve is included; the organic template comprises a compound represented by the following formula (I),

wherein the radical R₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight or branched alkylene and C_3-12Linear or branched oxaalkylene; a plurality of radicals R, equal to or different from each other, each independently selected from C_1-4A linear or branched alkyl group; x is OH;

the first oxide source is selected from at least one of a silicon dioxide source, a germanium dioxide source, a tin dioxide source, a titanium dioxide source and a zirconium dioxide source; the second oxide source is selected from at least one of an alumina source, a boron oxide source, an iron oxide source, a gallium oxide source, a rare earth oxide source, an indium oxide source, and a vanadium oxide source.

21. The process for making ethylbenzene of claim 20 in which the group R is₁And R₂Are the same or different from each other and are each independently selected from C_3-12Straight chain alkylene and C_3-12A linear oxaalkylene group.

22. The process for making ethylbenzene of claim 20 in which the group R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear or branched alkylene, the other being selected from C_3-12Straight or branched alkylene and C_3-12Straight or branched oxaalkylene.

23. The process for making ethylbenzene of claim 20 in which the group R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear alkylene and the other is selected from C_3-12Straight chain alkylene and C_3-12A linear oxaalkylene group.

24. The process for making ethylbenzene of claim 20 in which the group R is₁And R₂Are identical or different from each other, one of them being selected from C_3-12Linear alkylene and the other is selected from C_4-6Straight chain alkylene and C_4-6A linear oxaalkylene group.

25. The process according to claim 20, wherein the plurality of radicals R, equal to or different from each other, are each independently selected from methyl and ethyl.

26. The process for ethylbenzene production of claim 20 wherein the ethylene feed used is one or more of pure ethylene, refinery catalytically cracked dry gas containing ethylene, and refinery catalytically cracked dry gas containing ethylene.

27. The process for ethylbenzene production of claim 20 wherein the catalyst comprises a binder and the molecular sieve; the mass fraction of the molecular sieve is 10-95% by mass of the catalyst.

28. The process for ethylbenzene production of claim 27 wherein the catalyst is prepared by: mixing and kneading the molecular sieve raw powder, a silicon-containing compound and/or an aluminum-containing compound, nitric acid and deionized water for molding, drying, then burning out a template agent in air at 450-550 ℃, then exchanging in an ammonium salt aqueous solution at 80-90 ℃, and finally roasting and deaminating at 500-600 ℃ for 1-5 hours to obtain a catalyst; wherein the silicon-containing compound is selected from one or more of silica sol, methyl orthosilicate and ethyl orthosilicate, and the aluminum-containing compound is selected from one or more of pseudo-boehmite, SB powder, aluminum sol and aluminum isopropoxide; the ammonium salt is selected from one or more of ammonium nitrate, ammonium chloride and ammonium sulfate.

29. The process for ethylbenzene production of claim 28 wherein the catalyst is prepared using a mixture of a silicon-containing compound and an aluminum-containing compound in a molar ratio of silica to alumina of from 1:1 to 1: 2.

30. The process for making ethylbenzene according to claim 20, wherein the process for making ethylbenzene is carried out in a fixed bubble bed reactor, a fixed trickle bed reactor, or a slurry bed reactor.

31. The process for ethylbenzene production according to claim 20 wherein the alkylation reaction conditions are: reaction temperature is 150-280 ℃, and reactionThe reaction pressure is 1 MPa-4 MPa, and the molar ratio of benzene to ethylene is 1: 1-15: 1, weight hourly space velocity in terms of ethylene of 0.1h^-1～0.8h^-1。

32. The process for ethylbenzene production according to claim 20 wherein the alkylation reaction conditions are: the reaction temperature is 160-250 ℃, the reaction pressure is 1.2-3.6 MPa, and the molar ratio of benzene to ethylene is 3: 1-12: 1, weight hourly space velocity in terms of ethylene of 0.1h^-1～0.5h^-1。