阅读说明：本技术 加氢裂化催化剂及其制备方法和应用 (Hydrocracking catalyst, preparation method and application thereof ) 是由 杨平 庄立 聂红 胡志海 王轶凡 张毓莹 于 2019-10-30 设计创作，主要内容包括：本发明提供一种加氢裂化催化剂及其制备方法和应用。所述加氢裂化催化剂包括载体和负载在所述载体上的活性金属组分,所述载体包括基质和Y分子筛,其中,以所述加氢裂化催化剂为基准,以氧化物计,所述加氢裂化催化剂含有1～10wt％的Ⅷ族金属组分,2～40wt％的ⅥB族金属组分；载体中所述Y分子筛的含量为30～90wt％,基质的含量为10～70wt％；其中,所述Y分子筛的晶胞常数为2.415～2.440nm；所述Y分子筛的～(27)Al MAS NMR谱中化学位移为0±2ppm共振信号的峰面积占总峰面积的比例不大于4％；所述Y分子筛的强酸量占总酸量比例70％以上。本发明的加氢裂化催化剂用于催化柴油加氢裂化生产汽油或轻质芳烃过程,具有理想产物如汽油或轻质芳烃收率高、选择性好、汽油辛烷值高等特点。(The invention provides a hydrocracking catalyst, a preparation method and application thereof. The hydrocracking catalyst comprises a carrier and an active metal component loaded on the carrier, wherein the carrier comprises a matrix and a Y molecular sieve, and the hydrocracking catalyst contains 1-10 wt% of a VIII group metal component and 2-40 wt% of a VIB group metal component in terms of oxides based on the hydrocracking catalyst; the content of the Y molecular sieve in the carrier is 30-90 wt%, and the content of the matrix is 10-70 wt%; wherein the unit cell constant of the Y molecular sieve is 2.415-2.440 nm; of the Y molecular sieve 27 The proportion of the peak area of the resonance signal with the chemical shift of 0 +/-2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 4 percent; the strong acid content of the Y molecular sieve accounts for more than 70 percent of the total acid content. The hydrocracking catalyst of the invention is used for catalysisThe process for producing gasoline or light aromatic hydrocarbon by hydrocracking diesel oil has the characteristics of high yield, good selectivity, high gasoline octane number and the like of ideal products such as gasoline or light aromatic hydrocarbon.)

1. A hydrocracking catalyst, characterized in that the hydrocracking catalyst comprises a carrier and an active metal component loaded on the carrier, the carrier comprises a matrix and a Y molecular sieve,

wherein the hydrocracking catalyst is taken as a reference, and contains 1-10 wt% of a VIII group metal component and 2-40 wt% of a VIB group metal component in terms of oxides; based on the carrier, the content of the Y molecular sieve is 30-90 wt%, and the content of the matrix is 10-70 wt%;

wherein the unit cell constant of the Y molecular sieve is 2.415-2.440 nm; of the Y molecular sieve²⁷The proportion of the peak area of the resonance signal with the chemical shift of 0 +/-2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 4 percent; the strong acid content of the Y molecular sieve accounts for more than 70 percent of the total acid content.

2. The hydrocracking catalyst according to claim 1, wherein the Y molecular sieve has a unit cell constant of 2.422 to 2.438 nm; of the Y molecular sieve²⁷The ratio of the peak area of resonance signal with chemical shift of 0 + -2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 3Percent; the strong acid amount of the Y molecular sieve accounts for more than 75 percent of the total acid amount.

3. Hydrocracking catalyst according to claim 1, characterized in that the Y molecular sieve has a micropore specific surface area of 650m²A ratio of 700m or more, preferably 700m²More than g; the proportion of the mesoporous volume of the Y molecular sieve in the total pore volume is 30-50%, preferably 33-45%.

4. Hydrocracking catalyst according to any of claims 1 to 3, characterized in that the matrix is selected from one or more of alumina, silica and silica-alumina.

5. The hydrocracking catalyst according to any one of claims 1 to 3, wherein the hydrocracking catalyst contains 1 to 6 wt% of a group VIII metal component and 5 to 25 wt% of a group VIB metal component in terms of oxides based on the hydrocracking catalyst.

6. The hydrocracking catalyst according to any one of claims 1 to 3, wherein the Y molecular sieve is present in an amount of 45 to 80 wt% and the matrix is present in an amount of 20 to 55 wt%, based on the carrier.

7. The process for preparing a hydrocracking catalyst according to any one of claims 1 to 6, characterized by comprising:

uniformly mixing the Y molecular sieve and the matrix, molding, and roasting to obtain the carrier;

and (3) impregnating the carrier with a solution containing the active metal component, and drying and roasting to obtain the hydrocracking catalyst.

8. The method of claim 7, further comprising, prior to mixing the Y molecular sieve with the matrix, preparing the Y molecular sieve by:

mixing the NaY molecular sieve with ammonium salt and water to carry out primary ammonium exchange treatment to obtain a primary ammonium exchange molecular sieve;

carrying out first hydrothermal roasting treatment on the first ammonium exchange molecular sieve in a steam atmosphere to obtain a first water-roasted molecular sieve;

mixing the first water-baked molecular sieve with water, and adding a first dealuminizing agent to carry out first dealuminization treatment to obtain a first dealuminized molecular sieve;

carrying out second hydrothermal roasting treatment on the first dealuminized molecular sieve in a steam atmosphere to obtain a second hydrothermal roasted molecular sieve;

mixing the second water-baked molecular sieve with water, and adding a second dealuminizing agent for second dealuminization treatment to obtain a second dealuminized molecular sieve;

carrying out third hydrothermal roasting treatment on the second dealuminized molecular sieve in a steam atmosphere to obtain a third water-roasted molecular sieve;

mixing the third-time water-baked molecular sieve with water, and adding a third dealuminizing agent to carry out third dealuminizing treatment to obtain a third dealuminized molecular sieve; and

mixing the third dealuminized molecular sieve with water, adding a fourth dealuminizing agent for fourth dealuminization treatment, filtering and washing to obtain the Y molecular sieve,

wherein the ammonium salt is selected from one or more of ammonium chloride, ammonium nitrate, ammonium carbonate, ammonium bicarbonate, ammonium oxalate, ammonium sulfate and ammonium bisulfate, and the fourth dealuminating agent comprises a dealuminating agent containing silicon.

9. The method of claim 8, wherein the first, second and third dealuminating agents are each independently selected from one or more of organic acids selected from the group consisting of ethylenediaminetetraacetic acid, oxalic acid, citric acid and sulfosalicylic acid, inorganic acids selected from the group consisting of fluorosilicic acid, hydrochloric acid, sulfuric acid and nitric acid, and organic and inorganic salts selected from the group consisting of ammonium oxalate, ammonium fluoride, ammonium fluorosilicate and ammonium fluoroborate.

10. A method of producing as claimed in claim 8 wherein the silicon-containing dealuminating agent is fluorosilicic acid, ammonium fluorosilicate or a mixture of fluorosilicic acid and ammonium fluorosilicate.

11. The preparation method according to claim 8, wherein the fourth dealuminating agent further comprises an organic acid and/or an inorganic acid, and the mass ratio of the silicon-containing dealuminating agent to the organic acid and/or the inorganic acid is 0.02-0.3: 0-0.07, the organic acid is selected from one or more of ethylenediamine tetraacetic acid, oxalic acid, citric acid and sulfosalicylic acid, and the inorganic acid is selected from one or more of hydrochloric acid, sulfuric acid and nitric acid.

12. The production method according to claim 8, wherein the temperature of the first hydrothermal calcination treatment, the second hydrothermal calcination treatment, and the third hydrothermal calcination treatment is 350 to 700 ℃, the water vapor concentration is 1 to 100%, and the calcination time is 0.5 to 10 hours; the temperature of the first ammonium exchange treatment is room temperature to 95 ℃, and the treatment time is 0.5 to 5 hours; the temperature of the first dealuminization treatment is between room temperature and 90 ℃, and the treatment time is between 0.5 and 6 hours; the temperature of the second dealuminization treatment is between room temperature and 100 ℃, and the treatment time is between 0.5 and 6 hours; the temperature of the third dealuminization treatment is between room temperature and 100 ℃, and the treatment time is 0.5 to 6 hours; the temperature of the fourth dealuminization treatment is between room temperature and 100 ℃, and the treatment time is between 0.5 and 6 hours.

13. The production method according to any one of claims 8 to 12, characterized in that the ammonium salt is added in at least one of the first dealumination treatment, the second dealumination treatment, the third dealumination treatment and the fourth dealumination treatment.

14. The method according to claim 13, wherein in the first ammonium exchange treatment, the NaY molecular sieve: the ammonium salt: water 1: 0.3-1.0: 5-10; in the first dealumination treatment, the first water-calcined molecular sieve: the ammonium salt: the first dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10; in the second dealumination treatment, the second water-calcined molecular sieve: the ammonium salt: the second dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10; in the third dealumination treatment, the third water-calcined molecular sieve: the ammonium salt: the third dealuminizing agent: water 1: 0-0.70: 0.02-0.3: 5-10; in the fourth dealumination treatment, the third dealumination molecular sieve: the ammonium salt: the silicon-containing dealuminizing agent comprises the following components: water 1: 0-0.70: 0.02-0.3: 5 to 10.

15. Use of a hydrocracking catalyst according to any one of claims 1 to 6 in the production of high octane gasoline by a diesel hydrocracking reaction.

16. The use of claim 15, wherein the hydrocracking reaction is carried out by using catalytic diesel as raw material and adopting a fixed bed single-stage series process and a light diesel circulation process.

17. The use of claim 16, wherein the fixed bed single stage series process comprises a hydrofinishing reaction zone and a hydrocracking reaction zone, the catalytic diesel first enters the hydrofinishing reaction zone and then enters the hydrocracking reaction zone, and the reaction conditions of the hydrofinishing reaction zone and the hydrocracking reaction zone each independently comprise: the reaction temperature is 300-450 ℃, the reaction pressure is 4.0-10.0 MPa, the volume ratio of hydrogen to oil is 200-1500, and the volume airspeed is 0.5-2.5; the light diesel oil circulation ratio of the light diesel oil circulation process is 0-0.5.

Technical Field

The invention relates to the field of catalysis, in particular to a hydrocracking catalyst and a preparation method and application thereof.

Background

In recent years, with the development of economy in China, the structure of oil products is changed, the requirements of gasoline and aviation kerosene are increased, the increase of diesel oil demand is reduced, and even negative increase occurs; the consumption ratio of diesel and gasoline in China is gradually reduced since 2006. On the other hand, with the enhancement of environmental awareness of people, the requirements on the quality of oil products are more and more strict, the fuel oil standard is upgraded from national fourth to national sixth from 2015 to 2019, the indexes such as sulfur content, cetane number and polycyclic aromatic hydrocarbon and the like for diesel oil are more and more strict, and particularly, the upper limit of the polycyclic aromatic hydrocarbon content in the national six-vehicle diesel oil standard is reduced from 11% to 7%. This indicates that the cost of inferior secondary processed diesel fuels, such as catalytic diesel, with high aromatics content and low cetane number, to process to satisfactory diesel fuels, is increased. Therefore, the research on the efficient conversion of the inferior secondary processing diesel into high-value products required by the market is concerned. The polycyclic aromatic hydrocarbon for catalyzing diesel oil mainly comprises short-side chain bicyclic aromatic hydrocarbon and also comprises a small amount of short-side chain tricyclic aromatic hydrocarbon. Based on the conversion process of bicyclic and tricyclic aromatics, hydrocracking technology has been found to convert low-value polycyclic aromatics to high-value monocyclic aromatics such as alkylbenzenes, BTX, and the like. The nature of the catalyst is a key factor affecting the activity of the reaction and the selectivity of the product. In the prior art, many hydrocracking catalysts and methods for producing high-octane gasoline by hydrocracking catalytic diesel oil are reported, for example:

CN 201510761618.4 discloses a catalyst for producing gasoline by catalytic diesel oil hydrocracking and a preparation method thereof. It is characterized by that after the conventional catalyst carrier is formed, dried and roasted, the carbon-deposition reaction is implemented on the carrier, then the carbon-removing treatment is implemented, and finally the conventional method is adopted to make impregnation. The preparation method can adjust the infrared acid strength distribution of the catalyst so as to improve the naphtha yield in the hydrocracking process of the catalytic cracking diesel oil and maintain the high naphtha octane number. The method is specifically characterized in that the infrared acid amount is kept to be 0.4-0.6 mmol/L, wherein the infrared acid amount of strong acid at the temperature of more than 350 ℃ is not more than 0.08mmol/L, and the ratio of the infrared acid amount to the content of the strong acid at the temperature of more than 350 ℃ is 5-50.

CN 201510921122.9 discloses a method for producing clean diesel oil and light aromatic hydrocarbon from poor diesel oil, which is characterized in that the poor diesel oil is hydrofined, then aromatic hydrocarbon and sulfide are removed by simulated moving bed adsorption analysis, and the heavy aromatic hydrocarbon obtained by separation is subjected to hydro-upgrading to produce BTX light aromatic hydrocarbon, gasoline components and a small amount of light hydrocarbon. The hydrogenation modified catalyst is a molecular sieve catalyst loaded with noble metals of Pt, Pd and Re. From the published patent, the noble metal content on the catalyst is very low, 0.05 wt% to 0.5 wt%; the reaction pressure is also very low, 2-5 MPa.

CN 201110369112.0 discloses a catalyst for converting polycyclic aromatic hydrocarbon into monocyclic aromatic hydrocarbon and a method thereof, the catalyst comprises a mixture of 34.5-60 wt% FAU type zeolite and at least one molecular sieve selected from MOR, BEA, MFI or MCM-22, 39.5-65 wt% of at least one selected from gamma-alumina, eta-alumina or pseudo-boehmite is a binder and 0.05-0.9 wt% of at least one metal selected from Pt, Pd or Ir.

Although various catalysts for diesel hydrocracking have been disclosed so far, the following problems still remain in the art reported so far: the problems of low gasoline fraction yield, low RON, low yield of light aromatic hydrocarbon BTX and the like still need to optimize the property of the catalyst to improve the activity and the selectivity of an ideal reaction.

It is noted that the information disclosed in the foregoing background section is only for enhancement of background understanding of the invention and therefore it may contain information that does not constitute prior art that is already known to a person of ordinary skill in the art.

Disclosure of Invention

The invention aims to provide a catalyst with high polycyclic aromatic hydrocarbon ring-opening activity and high monocyclic aromatic hydrocarbon selectivity so as to improve the gasoline yield and the gasoline quality in the process of producing gasoline by hydrocracking diesel oil.

In order to achieve the purpose, the invention adopts the following technical scheme:

a hydrocracking catalyst comprises a carrier and an active metal component loaded on the carrier, wherein the carrier comprises a matrix and a Y molecular sieve,

wherein the hydrocracking catalyst is taken as a reference, and contains 1-10 wt% of a VIII group metal component and 2-40 wt% of a VIB group metal component in terms of oxides; based on the carrier, the content of the Y molecular sieve is 30-90 wt%, and the content of the matrix is 10-70 wt%;

wherein the unit cell constant of the Y molecular sieve is 2.415-2.440 nm; of the Y molecular sieve²⁷The proportion of the peak area of the resonance signal with the chemical shift of 0 +/-2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 4 percent; the strong acid content of the Y molecular sieve accounts for more than 70 percent of the total acid content.

In some embodiments, the Y molecular sieve has a unit cell constant of 2.422-2.438 nm; of the Y molecular sieve²⁷The proportion of the peak area of the resonance signal with the chemical shift of 0 +/-2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 3 percent; the strong acid amount of the Y molecular sieve accounts for more than 75 percent of the total acid amount.

In some embodiments, the Y molecular sieve has a micropore specific surface area of 650m²A ratio of 700m or more, preferably 700m²More than g; the proportion of the mesoporous volume of the Y molecular sieve in the total pore volume is 30-50%, preferably 33-45%.

In some embodiments, the matrix is selected from one or more of alumina, silica, and silica-alumina.

In some embodiments, the hydrocracking catalyst contains 1 to 6 wt% of the group VIII metal component and 5 to 25 wt% of the group VIB metal component, calculated as oxides, based on the hydrocracking catalyst.

In some embodiments, the Y molecular sieve is present in an amount of 45 to 80 wt% and the matrix is present in an amount of 20 to 55 wt%, based on the support.

In another aspect, the present invention provides a method for preparing the hydrocracking catalyst, comprising:

uniformly mixing the Y molecular sieve and the matrix, molding, and roasting to obtain the carrier;

and (3) impregnating the carrier with a solution containing the active metal component, and drying and roasting to obtain the hydrocracking catalyst.

In some embodiments, prior to mixing the Y molecular sieve with the matrix, further comprising preparing the Y molecular sieve by:

mixing the NaY molecular sieve with ammonium salt and water to carry out primary ammonium exchange treatment to obtain a primary ammonium exchange molecular sieve;

carrying out first hydrothermal roasting treatment on the first ammonium exchange molecular sieve in a steam atmosphere to obtain a first water-roasted molecular sieve;

mixing the first water-baked molecular sieve with water, and adding a first dealuminizing agent to carry out first dealuminization treatment to obtain a first dealuminized molecular sieve;

carrying out second hydrothermal roasting treatment on the first dealuminized molecular sieve in a steam atmosphere to obtain a second hydrothermal roasted molecular sieve;

mixing the second water-baked molecular sieve with water, and adding a second dealuminizing agent for second dealuminization treatment to obtain a second dealuminized molecular sieve;

carrying out third hydrothermal roasting treatment on the second dealuminized molecular sieve in a steam atmosphere to obtain a third water-roasted molecular sieve;

mixing the third-time water-baked molecular sieve with water, and adding a third dealuminizing agent to carry out third dealuminizing treatment to obtain a third dealuminized molecular sieve; and

mixing the third dealuminized molecular sieve with water, adding a fourth dealuminizing agent for fourth dealuminization treatment, filtering and washing to obtain the Y molecular sieve,

wherein the ammonium salt is selected from one or more of ammonium chloride, ammonium nitrate, ammonium carbonate, ammonium bicarbonate, ammonium oxalate, ammonium sulfate and ammonium bisulfate, and the fourth dealuminating agent comprises a dealuminating agent containing silicon.

In some embodiments, the first, second, and third dealuminating agents are each independently selected from one or more of organic acids selected from ethylenediaminetetraacetic acid, oxalic acid, citric acid, and sulfosalicylic acid, inorganic acids selected from fluorosilicic acid, hydrochloric acid, sulfuric acid, and nitric acid, and organic and inorganic salts selected from ammonium oxalate, ammonium fluoride, ammonium fluorosilicate, and ammonium fluoroborate.

In some embodiments, the silicon-containing dealuminating agent is fluorosilicic acid, ammonium fluorosilicate, or a mixture of fluorosilicic acid and ammonium fluorosilicate.

In some embodiments, the fourth dealuminating agent further comprises an organic acid and/or an inorganic acid, and the mass ratio of the silicon-containing dealuminating agent to the organic acid and/or the inorganic acid is 0.02-0.3: 0-0.07, the organic acid is selected from one or more of ethylenediamine tetraacetic acid, oxalic acid, citric acid and sulfosalicylic acid, and the inorganic acid is selected from one or more of hydrochloric acid, sulfuric acid and nitric acid.

In some embodiments, the first hydrothermal roasting treatment, the second hydrothermal roasting treatment and the third hydrothermal roasting treatment are performed at a temperature of 350 to 700 ℃, a water vapor concentration of 1 to 100%, and a roasting time of 0.5 to 10 hours; the temperature of the first ammonium exchange treatment is room temperature to 95 ℃, and the treatment time is 0.5 to 5 hours; the temperature of the first dealuminization treatment is between room temperature and 90 ℃, and the treatment time is between 0.5 and 6 hours; the temperature of the second dealuminization treatment is between room temperature and 100 ℃, and the treatment time is between 0.5 and 6 hours; the temperature of the third dealuminization treatment is between room temperature and 100 ℃, and the treatment time is 0.5 to 6 hours; the temperature of the fourth dealuminization treatment is between room temperature and 100 ℃, and the treatment time is between 0.5 and 6 hours.

In some embodiments, the ammonium salt is added to at least one of the first dealumination treatment, the second dealumination treatment, the third dealumination treatment and the fourth dealumination treatment.

In some embodiments, the NaY molecular sieve in the first ammonium exchange treatment is: the ammonium salt: water 1: 0.3-1.0: 5-10; in the first dealumination treatment, the first water-calcined molecular sieve: the ammonium salt: the first dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10; in the second dealumination treatment, the second water-calcined molecular sieve: the ammonium salt: the second dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10; in the third dealumination treatment, the third water-calcined molecular sieve: the ammonium salt: the third dealuminizing agent: water 1: 0-0.70: 0.02-0.3: 5-10; in the fourth dealumination treatment, the third dealumination molecular sieve: the ammonium salt: the silicon-containing dealuminizing agent comprises the following components: water 1: 0-0.70: 0.02-0.3: 5 to 10.

On the other hand, the invention provides the application of the hydrocracking catalyst in the production of high-octane gasoline by diesel oil hydrocracking reaction.

In some embodiments, the hydrocracking reaction is carried out using a fixed bed single stage series and light diesel recycle process, starting with catalytic diesel.

In some embodiments, the fixed bed single stage series process comprises a hydrofinishing reaction zone and a hydrocracking reaction zone, the catalytic diesel first enters the hydrofinishing reaction zone and then enters the hydrocracking reaction zone, and the reaction conditions of the hydrofinishing reaction zone and the hydrocracking reaction zone each independently comprise: the reaction temperature is 300-450 ℃, the reaction pressure is 4.0-10.0 MPa, the volume ratio of hydrogen to oil is 200-1500, and the volume airspeed is 0.5-2.5; the light diesel oil circulation ratio of the light diesel oil circulation process is 0-0.5

The hydrocracking catalyst provided by the invention has the characteristics that the catalyst has high selective hydrogenation saturation activity of polycyclic aromatic hydrocarbon, strong ring opening performance of naphthenic ring and high retention degree of monocyclic aromatic hydrocarbon by modifying the molecular sieve and using the Y molecular sieve with high silicon-aluminum ratio, less non-framework aluminum, large specific surface area, rich secondary pores and high strong acid center ratio, and the synergy and matching of the hydrogenation function and the acidic function are enhanced while the ring opening and cracking performance of the catalyst is improved.

Detailed Description

The technical solution of the present invention is further explained below according to specific embodiments. The scope of protection of the invention is not limited to the following examples, which are set forth for illustrative purposes only and are not intended to limit the invention in any way.

In the present invention, anything or matters not mentioned is directly applicable to those known in the art without any change except those explicitly described. Moreover, any embodiment described herein may be freely combined with one or more other embodiments described herein, and the technical solutions or ideas thus formed are considered part of the original disclosure or original description of the present invention, and should not be considered as new matters not disclosed or contemplated herein, unless a person skilled in the art would consider such combination to be clearly unreasonable.

All features disclosed in this invention may be combined in any combination and such combinations are understood to be disclosed or described herein unless a person skilled in the art would consider such combinations to be clearly unreasonable. The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

According to a first aspect of the present invention, there is provided a hydrocracking catalyst comprising a support and an active metal component supported on the support, the support comprising a matrix and a molecular sieve.

In the catalyst of the invention, the substrate is a heat-resistant inorganic oxide selected from one or more of alumina, silica and silica-alumina. The alumina used in the invention is one or more transition phase alumina selected from gamma, eta, theta, delta and chi, also can be one or more transition phase alumina selected from gamma, eta, theta, delta and chi containing one or more additive components selected from silicon, titanium, magnesium, boron, zirconium, thorium, niobium and rare earth, and is preferably gamma-alumina and gamma-alumina containing one or more additive components selected from silicon, phosphorus, titanium, magnesium, boron, zirconium, thorium, niobium and rare earth. They may be commercially available or obtained by any of the existing methods.

The unit cell constant of the Y molecular sieve used in the catalyst is 2.415-2.440 nm, and the unit cell constant is preferably 2.422-2.438 nm; specific surface area of micropores is 650m²A ratio of 700m or more, preferably 700m²More than g; the mesopore volume accounts for 30 to 50 percent of the total pore volume, and preferably 33 to 45 percent; of molecular sieves²⁷The proportion of the peak area of the resonance signal with the chemical shift of 0 +/-2 ppm in the Al MAS NMR spectrum to the total peak area is not more than 4 percent, and preferably not more than 3 percent; the proportion of the strong acid amount of the molecular sieve to the total acid amount is 70% or more, preferably 75% or more.

The strong acid of the Y molecular sieve in the invention is NH₃Temperature programmed desorption (NH)₃Acid with desorption temperature higher than 320 ℃ in the TPD) curve, the ratio of the acid amount of strong acid to the acid amount is NH₃The desorption temperature in the TPD results is greater than the ratio of the amount of strong acid to the amount of acid at 320 ℃.

Based on the carrier, the content of the Y molecular sieve is 30-90 wt%, the content of the matrix is 10-70 wt%, and preferably, the content of the Y molecular sieve is 45-80 wt%, and the content of the matrix is 20-55 wt%.

In the catalyst of the present invention, the active metal component comprises at least one metal component selected from group VIII and at least one metal component selected from group VIB. The metal component of group VIII may be iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, etc., and the metal component of group VIB may be chromium, molybdenum, tungsten, etc. The active metal component is usually supported on the support in the form of a metal oxide.

Based on a hydrocracking catalyst, the hydrocracking catalyst contains 1-10 wt% of a VIII group metal component, 2-40 wt% of a VIB group metal component and the balance of a carrier in terms of oxides; preferably, the hydrocracking catalyst contains 1-6 wt% of VIII group metal component, 5-25 wt% of VIB group metal component and the balance of carrier.

The hydrocracking catalyst of the invention can be prepared by the following method:

uniformly mixing the Y molecular sieve and the matrix, molding, and roasting to obtain a carrier;

preparing an impregnation solution of a compound containing an active metal component; and

impregnating the carrier by using the impregnating solution, and drying and roasting to obtain the hydrocracking catalyst.

In the catalyst of the invention, the carrier is made of molecular sieve and matrix, and can be made into various easy-to-handle molded objects according to different requirements, such as microspheres, spheres, tablets or strips. The shaping can be carried out by conventional methods, for example, by extruding the molecular sieve and the matrix into strips and calcining the strips. When the carrier is extruded and molded, a proper amount of extrusion aid and/or adhesive can be added into the carrier, and then the carrier is extruded and molded. The kind and amount of the extrusion aid and the peptizing agent are well known to those skilled in the art, for example, common extrusion aid may be one or more selected from sesbania powder, methyl cellulose, starch, polyvinyl alcohol, and polyvinyl alcohol.

The supporting method is not particularly limited in the present invention on the premise that it is sufficient to support the active metal component on the carrier, and a preferable method is an impregnation method comprising preparing an impregnation solution of the metal component-containing compound and thereafter impregnating the carrier with the solution. The impregnation method is a conventional method, and for example, it may be an excess liquid impregnation method, a pore saturation method impregnation method. Wherein the specified amount of catalyst can be prepared by adjusting and controlling the concentration, amount or support amount of the impregnation solution containing the metal component, as will be readily understood and realized by those skilled in the art.

The compound containing the metal component selected from the VIB group is selected from one or more soluble compounds thereof, such as one or more of molybdenum oxide, molybdate and paramolybdate, preferably molybdenum oxide, ammonium molybdate and paramolybdate; one or more of tungstate, metatungstate and ethyl metatungstate, preferably ammonium metatungstate and ethyl metatungstate.

The compound containing the metal component selected from the group VIII is selected from one or more soluble compounds thereof, such as one or more soluble complexes of cobalt nitrate, cobalt acetate, basic cobalt carbonate, cobalt chloride and cobalt, preferably cobalt nitrate and basic cobalt carbonate; one or more of nickel nitrate, nickel acetate, basic nickel carbonate, nickel chloride and soluble complex of nickel, preferably nickel nitrate and basic nickel carbonate.

The preparation of the Y molecular sieve is also included prior to mixing the acidic component with the matrix. The Y molecular sieve is prepared by taking an NaY molecular sieve as a raw material and performing multiple times of exchange, dealumination and three times of hydrothermal roasting, wherein dealumination treatment is performed at least once before the second hydrothermal roasting and the third hydrothermal roasting, dealumination is performed at least twice continuously after the third hydrothermal roasting, and a silicon-containing dealumination agent is used in the last dealumination process.

Specifically, the preparation method of the Y molecular sieve of the invention can comprise the following steps:

mixing the NaY molecular sieve with ammonium salt and water to carry out primary ammonium exchange treatment to obtain a primary ammonium exchange molecular sieve;

carrying out first hydrothermal roasting treatment on the first-time ammonium exchange molecular sieve in a steam atmosphere to obtain a first-time water-roasted molecular sieve;

mixing the first water-baked molecular sieve with water, and adding a first dealuminizing agent to carry out first dealuminization treatment to obtain a first dealuminized molecular sieve;

carrying out second hydrothermal roasting treatment on the first dealuminized molecular sieve in a steam atmosphere to obtain a second hydrothermal roasted molecular sieve;

mixing the second water-baked molecular sieve with water, and adding a second dealuminizing agent for second dealuminization treatment to obtain a second dealuminized molecular sieve;

carrying out third hydrothermal roasting treatment on the second dealuminized molecular sieve in a steam atmosphere to obtain a third hydrothermal roasted molecular sieve;

mixing the third-time water-baked molecular sieve with water, and adding a third dealuminizing agent to carry out third dealuminizing treatment to obtain a third dealuminized molecular sieve; and

mixing the third dealuminized molecular sieve with water, adding a fourth dealuminizing agent for fourth dealuminization treatment, filtering and washing to obtain a Y molecular sieve,

wherein the fourth dealuminizing agent comprises a silicon-containing dealuminizing agent.

In the production method of the present invention, the ammonium salts used in the ammonium exchange treatment are each independently one or more selected from the group consisting of ammonium chloride, ammonium nitrate, ammonium carbonate, ammonium hydrogencarbonate, ammonium oxalate, ammonium sulfate and ammonium bisulfate.

In the preparation method of the invention, the first ammonium exchange treatment is to mix NaY zeolite (namely NaY molecular sieve) with ammonium salt and water according to the weight ratio of NaY molecular sieve: ammonium salt: water 1: 0.3-1.0: 5-10 to obtain slurry, treating the slurry at room temperature to 95 ℃ for 0.5-5 hours, washing and drying the slurry to obtain the first ammonium exchange molecular sieve. Wherein, the NaY molecular sieve is based on the weight of a dry basis (the weight of the molecular sieve after being calcined for 1 hour at 800 ℃ in the invention).

In the preparation method, the first hydrothermal roasting treatment is to roast the first ammonium exchange molecular sieve for 0.5 to 10 hours at the temperature of 350 to 700 ℃ in the atmosphere of 1 to 100 percent of water vapor to obtain the first hydrothermal roasting molecular sieve.

In the preparation method of the invention, the first dealumination treatment is carried out according to the following steps of first water roasting molecular sieve: optional ammonium salts: a first dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10, mixing water with the first-time water-baked molecular sieve and optional ammonium salt, adding a first dealumination agent, treating at room temperature to 90 ℃ for 0.5-6 hours, filtering, and washing to obtain a first-time dealumination molecular sieve, wherein the first-time water-baked molecular sieve is based on dry weight.

In the preparation method, the second hydrothermal roasting treatment is to roast the first dealuminized molecular sieve for 0.5 to 10 hours at the temperature of 350 to 700 ℃ in the atmosphere of 1 to 100 percent of water vapor to obtain the second hydrothermal roasted molecular sieve.

In the preparation method of the invention, the second dealumination treatment is carried out according to the following steps of water roasting molecular sieve for the second time: optional ammonium salts: a second dealuminizing agent: water 1: 0-0.50: 0.02-0.3: 5-10, mixing water with the second-time water-baked molecular sieve and optional ammonium salt, adding a second dealuminizing agent, treating at room temperature to 100 ℃ for 0.5-6 hours, filtering, and washing to obtain a second-time dealuminized molecular sieve, wherein the second-time water-baked molecular sieve is based on dry weight.

In the preparation method, the third hydrothermal roasting treatment is to roast the second dealuminized molecular sieve for 0.5 to 10 hours at the temperature of 350 to 700 ℃ in the atmosphere of 1 to 100 percent of water vapor to obtain the third hydrothermal roasted molecular sieve.

In the preparation method of the invention, the third dealuminization treatment is carried out according to the following steps of water roasting molecular sieve: optional ammonium salts: a third dealuminizing agent: water 1: 0-0.70: 0.02-0.3: 5-10, mixing water with the third-time water-baked molecular sieve and optional ammonium salt, adding a third dealuminizing agent, treating at room temperature to 100 ℃ for 0.5-6 hours, filtering, and washing to obtain a third-time dealuminized molecular sieve, wherein the third-time water-baked molecular sieve is based on dry weight.

In the preparation method of the invention, the fourth dealumination treatment is carried out according to the third dealumination molecular sieve: optional ammonium salts: silicon-containing dealuminizing agent: organic and/or inorganic acids: water 1: 0-0.70: 0.02-0.3: 0-0.07: 5-10, mixing the third dealuminized molecular sieve with optional ammonium salt and water, adding a fourth dealuminizing agent (at least comprising a silicon-containing dealuminizing agent, and further comprising organic acid and/or inorganic acid), treating at room temperature-100 ℃ for 0.5-6 hours, filtering and washing to obtain the fourth dealuminized molecular sieve, wherein the third dealuminized molecular sieve is based on dry weight.

In the preparation method of the present invention, the first dealuminating agent, the second dealuminating agent and the third dealuminating agent may be the same or different and are each independently selected from one or more of organic acids, inorganic acids and organic and inorganic salts, wherein the organic acids are selected from ethylenediaminetetraacetic acid, oxalic acid, citric acid and sulfosalicylic acid, the inorganic acids are selected from fluorosilicic acid, hydrochloric acid, sulfuric acid and nitric acid, and the organic and inorganic salts are selected from ammonium oxalate, ammonium fluoride, ammonium fluorosilicate and ammonium fluoroborate.

In the preparation method of the invention, the dealumination agent used in the last dealumination treatment (i.e. the fourth dealumination treatment) comprises a silicon-containing dealumination agent, and can further comprise organic acid and/or inorganic acid, wherein the silicon-containing dealumination agent is fluosilicic acid, ammonium fluosilicate or a mixture of fluosilicic acid and ammonium fluosilicate, the organic acid in the organic acid and/or the inorganic acid is selected from one or more of ethylenediamine tetraacetic acid, oxalic acid, citric acid and sulfosalicylic acid, and the inorganic acid is selected from one or more of hydrochloric acid, sulfuric acid and nitric acid.

The Y molecular sieve is prepared by multiple dealumination and three times of water roasting, aluminum vacancies formed in the dealumination process can be filled with silicon as much as possible in the water roasting process, generated non-framework aluminum is gradually stripped through multiple dealumination, and the three times of hydrothermal roasting and the multiple dealumination supplement each other, so that the completeness of crystals is kept, and more strong acid centers are reserved.

Therefore, the Y molecular sieve has high silicon-aluminum ratio, less non-framework aluminum, high strong acid center ratio, large specific surface area, rich secondary pores, higher reaction activity in hydrocarbon cracking reactions such as hydrocracking and the like, less secondary reactions, good ring-opening reaction selectivity, good acid stability and slow inactivation.

On the other hand, the invention also provides the application of the hydrocracking catalyst in producing high-octane gasoline by hydrocracking diesel oil.

Specifically, catalytic diesel oil is used as a raw material, the hydrocracking catalyst is utilized, and a fixed bed single-stage series connection and light diesel oil circulation process are adopted to carry out hydrocracking reaction to produce high-octane gasoline.

The catalytic diesel oil treated by the invention is a light cycle oil product of a catalytic cracking unit in a petroleum refining process, wherein the content of aromatic hydrocarbon is high, and bicyclic aromatic hydrocarbon is taken as a main component. The dry point of the catalytic diesel is more than 330 ℃, and the dry point is preferably more than 350 ℃.

The fixed bed single-stage series process usually comprises a hydrofining reaction zone and a hydrocracking reaction zone, catalytic diesel firstly enters the hydrofining reaction zone to remove impurities such as S, N and carry out a hydrogenation saturation reaction of aromatic hydrocarbons, then hydrofining effluent enters the hydrocracking reaction zone to carry out ring opening and cracking reactions to generate high-octane gasoline components such as alkylbenzene and BTX and the like, and a part of obtained products is used as raw materials through a light diesel oil circulation process and then enters the hydrofining reaction zone and the hydrocracking reaction zone in the fixed bed single-stage series process to carry out a reaction.

The reaction conditions of the hydrofinishing reaction zone and the hydrocracking reaction zone may be the same or different and each independently comprise the following reaction conditions: the reaction temperature is 300-450 ℃, the reaction pressure is 4.0-10.0 MPa, the volume ratio of hydrogen to oil is 200-1500, and the volume airspeed is 0.5-2.5; the light diesel oil circulation ratio of the light diesel oil circulation process is 0-0.5.

The catalyst used in the hydrofinishing reaction zone in the present invention may be any of a variety of commercial catalysts or may be prepared according to techniques known in the art.

Researches find that the process of converting the polycyclic aromatic hydrocarbon into the high-octane gasoline component or the light aromatic hydrocarbon mainly comprises the ideal reactions of selective hydrogenation saturation of the polycyclic aromatic hydrocarbon, ring opening of naphthenic rings, side chain breaking of alkyl aromatic hydrocarbon and the like. Researches find that secondary pores of the acidic component are increased within a certain range, the surface area of the molecular sieve is increased, the smoothness of a pore channel is improved, the accessibility of reaction molecules on an acidic active center is favorably improved, and the ring-opening and cracking activity of the reaction molecules is further improved; meanwhile, the surface property and the pore structure of the molecular sieve can also adjust the dispersion of metal components and the structure of an active phase, so that the hydrogenation performance of the catalyst is optimized, the synergistic effect of a hydrogenation center and an acid center on the catalyst is enhanced, and the selectivity of selective hydrogenation saturation, selective ring opening and cracking reaction of the polycyclic aromatic hydrocarbon is improved.

The hydrocracking catalyst provided by the invention has the characteristics that through modifying the molecular sieve, the Y molecular sieve with high silicon-aluminum ratio, less non-framework aluminum, large specific surface area, rich secondary pores and high strong acid center ratio is used, the synergy and matching of the hydrogenation function and the acidic function are enhanced while the ring opening and cracking performance of the catalyst is improved, so that the catalyst has the characteristics of high polycyclic aromatic hydrocarbon hydrogenation saturation activity, strong naphthenic ring opening performance and high monocyclic aromatic hydrocarbon retention degree, and when the catalyst is used for producing gasoline or light aromatic hydrocarbon by hydrocracking poor diesel, the component ratio of high-octane gasoline can be improved, and the light product is less and the chemical hydrogen consumption is low.

The present invention will be described in detail with reference to examples, but the scope of the present invention is not limited thereto.

Examples

Reagents, instruments and tests

In the following examples, preparations and comparative examples, the specifications of the raw materials used are as follows:

NaY molecular sieve, industrial product, silicon-aluminium ratio is greater than 4.7, crystallinity is greater than 85%

Sulfuric acid, chemical purity

Hydrochloric acid, chemical purity

Nitric acid, chemical purity

Oxalic acid, solid, chemically pure

Fluosilicic acid, technical grade

Ammonium nitrate, chemical purity

Ammonium chloride, chemical purity

Ammonium oxalate, chemical purity

Ammonium sulfate, chemical purity

In the following examples, preparations and comparative examples, the apparatus and the test methods involved are as follows:

the cell constants were measured by X-ray diffraction (XRD) using RIPP145-90 standard method (see "analytical methods in petrochemical industry (RIPP test method)", Yangshui et al, scientific Press, 1990 edition).

Measuring the micropore specific surface area of the molecular sieve by adopting a nitrogen adsorption BET specific surface area method; the mesoporous refers to a molecular sieve pore canal with the pore diameter larger than 2 nanometers and smaller than 50 nanometers, and the pore volume is determined by adopting a GB/T5816-.

²⁷The Al MAS NMR is tested by a Bruker Avance III 500MHz nuclear magnetic resonance instrument, and each peak area is calculated by an integration method after a resonance peak spectrogram is subjected to peak-splitting fitting.

The acid amount is NH₃-the TPD method is carried out,see methods for solid catalyst research, petrochemical, 30(12), 2001: 952 "in which the amount of strong acid refers to NH₃The peak temperature of desorption peak is larger than the acid center number above 320 ℃.

The chemical silica-alumina ratio was measured by X-ray fluorescence. Namely, the content of the silicon oxide and the aluminum oxide is calculated, and the content of the silicon oxide and the aluminum oxide is measured by adopting the GB/T30905-2014 standard method.

The kind and content of each metal element in the catalyst were measured by an X-ray fluorescence spectrum analysis method specified in RIPP 132-92 (compiled in methods of petrochemical engineering (RIPP experiments), Yangroi, etc., science publishers, 1 st edition at 1990, 9 months, p. 371-. When the catalyst was tested, a sample of the catalyst was stored under an argon atmosphere.

The composition of the catalyst after calcination is the composition of a sample obtained by calcining the catalyst at 400 to 600 ℃ for 4 hours in an atmospheric atmosphere.

Preparation example 1 preparation of molecular Sieve Y-1

(1) Exchanging NaY zeolite serving as a raw material by using an ammonium sulfate solution, wherein the treatment conditions are as follows: according to NaY molecular sieve (dry basis): ammonium sulfate: water 1: 1.0: 10, exchange at 90 ℃ for 2h, filter, wash with deionized water, and dry at 120 ℃ for 4 h.

(2) And (2) carrying out first hydrothermal roasting treatment on the molecular sieve obtained in the step (1), wherein the roasting temperature is 520 ℃, and roasting for 2h in a 100% steam atmosphere.

(3) And (3) mixing the molecular sieve obtained in the step (2) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: ammonium chloride: water 1: 0.06: 0.40: 9, pulping the molecular sieve by adding water, slowly dripping 20 percent sulfuric acid, controlling the dripping time for 30min, heating, treating at 70 ℃ for 40min, filtering, washing by deionized water, and drying at 120 ℃ for 4 h.

(4) And (4) carrying out second hydrothermal roasting treatment on the molecular sieve obtained in the step (3), wherein the roasting temperature is 620 ℃, and roasting for 2 hours in a 100% steam atmosphere.

(5) And (3) mixing the molecular sieve obtained in the step (4) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: water 1: 0.09: and 8, adding water into the molecular sieve, pulping, slowly dropwise adding 20% sulfuric acid, controlling the dropwise adding time for 30min, heating to 70 ℃, treating for 60min, filtering, washing with deionized water, and drying at 120 ℃ for 4 h.

(6) And (5) carrying out a third hydrothermal roasting treatment on the molecular sieve obtained in the step (5), wherein the roasting temperature is 650 ℃, and roasting for 2 hours in a 100% water vapor atmosphere.

(7) And (3) mixing the molecular sieve obtained in the step (7) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: water 1: 0.09: and 8, adding water into the molecular sieve, pulping, slowly dropwise adding 30% sulfuric acid, controlling the dropwise adding time for 40min, heating, treating at 70 ℃ for 60min, filtering, and washing with deionized water.

(8) And (3) mixing the molecular sieve obtained in the step (7) according to the following molecular sieve: ammonium sulfate: fluosilicic acid, sulfuric acid: H2O is the proportion of 1:0.2:0.05:0.02:8, the molecular sieve is firstly added with water and pulped, then ammonium sulfate is added, 30% fluosilicic acid and 20% sulphuric acid are slowly dripped, the dripping time is controlled for 40min, the molecular sieve Y-1 is obtained after being treated for 90min at 80 ℃ after being heated, and the molecular sieve Y-1 is obtained after being filtered and washed by deionized water, wherein each parameter is shown in Table 1.

Preparation example 2 preparation of molecular Sieve Y-2

(1) Exchanging NaY zeolite serving as a raw material by using an ammonium sulfate solution, wherein the treatment conditions are as follows: according to NaY molecular sieve (dry basis): ammonium sulfate: water 1:0.5: 7, exchange at 80 ℃ for 1h, filter, wash with deionized water, and dry at 120 ℃ for 4 h.

(2) And (2) carrying out first hydrothermal roasting treatment on the molecular sieve obtained in the step (1), wherein the roasting temperature is 670 ℃, and roasting for 2h in a 100% steam atmosphere.

(3) And (3) mixing the molecular sieve obtained in the step (2) according to the mass ratio of the molecular sieve (dry basis): oxalic acid: ammonium nitrate: water 1: 0.20: 0.40: 9, firstly adding water into the molecular sieve for pulping, adding ammonium nitrate and oxalic acid under stirring at room temperature, stirring for 60min, filtering, washing twice by deionized water, and drying at 120 ℃ for 3 h.

(4) And (4) carrying out second hydrothermal roasting treatment on the molecular sieve obtained in the step (3), wherein the roasting temperature is 645 ℃, and roasting for 2.5 hours in a 100% steam atmosphere.

(5) Adding 7 times of water into the molecular sieve obtained in the step (4), pulping, heating the pulp to 60 ℃, and then adding the following components in percentage by weight: nitric acid: ammonium oxalate: water 1: 0.13: 0.2, preparing ammonium oxalate, nitric acid and water into a solution, adding the aqueous solution into the molecular sieve slurry, controlling the dropping time to be 30min, continuously stirring at 60 ℃ for 40min, filtering, washing by deionized water, and drying at 105 ℃ for 2 h.

(6) And (5) carrying out a third hydrothermal roasting treatment on the molecular sieve obtained in the step (5), wherein the roasting temperature is 670 ℃, and roasting for 2h in a 100% water vapor atmosphere.

(7) And (3) mixing the molecular sieve obtained in the step (6) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: ammonium nitrate: water 1: 0.13: 0.30: 9, firstly adding a proper amount of water into the molecular sieve, pulping, then adding ammonium nitrate, then adding 30% sulfuric acid aqueous solution at a constant speed, controlling the dropping time for 40min, heating, treating at 70 ℃ for 60min, filtering, washing by deionized water, and drying at 120 ℃ for 4 h.

(8) And (3) mixing the molecular sieve obtained in the step (7) according to the following molecular sieve: ammonium sulfate: h2SiF 6: H2O ═ 1:0.2: 0.15: 7, adding water into the molecular sieve, pulping, adding ammonium sulfate, slowly adding 30% fluosilicic acid dropwise, controlling the dropwise adding time for 60min, heating, treating at 60 ℃ for 50min, filtering, washing with deionized water, and drying at 120 ℃ to obtain the molecular sieve Y-2, wherein all parameters are shown in table 1.

Preparation example 3 preparation of molecular Sieve Y-3

(1) Exchanging NaY zeolite serving as a raw material with an ammonium chloride solution, wherein the treatment conditions are as follows: according to NaY molecular sieve (dry basis): ammonium chloride: water 1: 0.7: 10, exchange at 85 ℃ for 1h, filter, wash with deionized water, and dry at 120 ℃ for 4 h.

(2) And (2) carrying out first hydrothermal roasting treatment on the molecular sieve obtained in the step (1), wherein the roasting temperature is 600 ℃, and roasting for 2h in a 100% steam atmosphere.

(3) And (3) mixing the molecular sieve obtained in the step (2) according to the mass ratio of the molecular sieve (dry basis): citric acid: sulfuric acid: water 1: 0.15: 0.05: and 8, adding water into the molecular sieve, pulping, heating, adding 20% sulfuric acid at a constant speed at 70 ℃ under stirring, controlling the dropping time for 30min, adding 20% citric acid aqueous solution, controlling the dropping time for 20min, continuously stirring at 70 ℃ for 1h after the addition is finished, filtering, washing with deionized water, and drying at 120 ℃ for 4 h.

(4) And (4) carrying out second hydrothermal roasting treatment on the molecular sieve obtained in the step (3), wherein the roasting temperature is 600 ℃, and roasting for 2 hours in a 100% steam atmosphere.

(5) And (3) mixing the molecular sieve obtained in the step (4) according to the mass ratio of the molecular sieve (dry basis): hydrochloric acid: ammonium sulfate: water 1: 0.06: 0.1: 10, adding water into the molecular sieve, pulping, adding ammonium sulfate, stirring uniformly, slowly dropwise adding hydrochloric acid with the concentration of 15%, controlling the dropwise adding time to be 1h, heating to 60 ℃, treating for 40min, filtering, washing with deionized water, and drying at 120 ℃ for 4 h.

(6) And (4) carrying out third hydrothermal roasting treatment on the molecular sieve obtained in the step (5), wherein the roasting temperature is 550 ℃, and roasting for 3 hours in a 100% water vapor atmosphere.

(7) And (3) mixing the molecular sieve obtained in the step (6) according to the mass ratio of the molecular sieve (dry basis): hydrochloric acid: oxalic acid: ammonium sulfate: water 1: 0.05: 0.19: 0.1: 10, adding water into the molecular sieve, pulping, adding ammonium sulfate, slowly dripping hydrochloric acid with the concentration of 10%, controlling the dripping time for 40min, adding oxalic acid, heating, treating at 70 ℃ for 60min, filtering, and washing with deionized water.

(8) Sieving the molecular sieve obtained in the step (7) according to a molecular sieve; ammonium chloride: fluosilicic acid, hydrochloric acid: H2O is 1:0.5:0.03:0.008:10, the molecular sieve is firstly pulped by adding water, ammonium chloride is added, simultaneously, 30% fluosilicic acid and 20% hydrochloric acid are slowly dripped, the dripping time is controlled for 60min, the temperature is increased, the molecular sieve is treated for 50min at 60 ℃, and the molecular sieve Y-3 is obtained by filtering and washing by deionized water, wherein all parameters are shown in Table 1.

Preparation example 4 preparation of molecular Sieve Y-4

(1) Exchanging NaY zeolite serving as a raw material by using an ammonium sulfate solution, wherein the treatment conditions are as follows: according to NaY molecular sieve (dry basis): ammonium sulfate: water 1: 1.0: 10, exchange at 90 ℃ for 2h, filter, wash with deionized water, and dry at 120 ℃ for 4 h.

(2) And (2) carrying out first hydrothermal roasting treatment on the molecular sieve obtained in the step (1), wherein the roasting temperature is 520 ℃, and roasting for 2h in a 100% steam atmosphere.

(3) And (3) mixing the molecular sieve obtained in the step (2) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: ammonium chloride: water 1: 0.06: 0.40: 9, pulping the molecular sieve by adding water, slowly dripping 20 percent sulfuric acid, controlling the dripping time for 30min, heating, treating at 70 ℃ for 40min, filtering, washing by deionized water, and drying at 120 ℃ for 4 h.

(4) And (4) carrying out second hydrothermal roasting treatment on the molecular sieve obtained in the step (3), wherein the roasting temperature is 620 ℃, and roasting for 2 hours in a 100% steam atmosphere.

(5) And (3) mixing the molecular sieve obtained in the step (4) according to the mass ratio of the molecular sieve (dry basis): sulfuric acid: water 1: 0.09: and 8, adding water into the molecular sieve, pulping, slowly dropwise adding 20% sulfuric acid, controlling the dropwise adding time for 30min, heating to 70 ℃, treating for 60min, filtering, washing with deionized water, and drying at 120 ℃ for 4 h.

(6) And (5) carrying out a third hydrothermal roasting treatment on the molecular sieve obtained in the step (5), wherein the roasting temperature is 650 ℃, and roasting for 2 hours in a 100% water vapor atmosphere.

(7) And (3) mixing the molecular sieve obtained in the step (7) according to the mass ratio of the molecular sieve (dry basis): ammonium sulfate: fluosilicic acid: sulfuric acid: h₂Adding water into a molecular sieve, pulping, adding ammonium sulfate, slowly dropwise adding 30% fluosilicic acid and 20% sulfuric acid, controlling the dropwise adding time for 40min, heating, treating at 80 ℃ for 90min, filtering, and washing with deionized water.

(8) And (3) mixing the molecular sieve obtained in the step (7) according to the following molecular sieve: ammonium sulfate: fluosilicic acid, sulfuric acid: h₂Adding water into the molecular sieve for pulping, adding ammonium sulfate, slowly dropwise adding 30% fluosilicic acid and 20% sulfuric acid, controlling the dropwise adding time for 40min, heating, treating at 80 ℃ for 90min, filtering, and washing with deionized water to obtain the molecular sieve Y-4, wherein all parameters are shown in Table 1.

TABLE 1 parameters of the respective molecular sieves in the preparation examples

Molecular sieves	Unit cell constant/nm	Fraction of mesopores%	Proportion of strong acid/%)	Specific surface area of micropores/(m)2/g)	A0±2ppm/AGeneral assembly/％*
						Y-1	2.426	42	80	685	3.2
Y-2	2.420	36	75	710	4.0
						Y-3	2.434	40	77	674	1.0
Y-4	2.423	39	84	700	1.0
						D-1	2.453	20	61	617	7.2

Note: denotes²⁷The ratio of the peak area of the resonance signal with a chemical shift of 0. + -.2 ppm in the Al MAS NMR spectrum to the total peak area.

Example 1

Weighing 128.6 g of pseudoboehmite (prepared by catalyst Changling division) with a dry basis of 70% and 134.1 g of molecular sieve Y-1 (prepared by preparation example 1) with a dry basis of 82%, uniformly mixing, extruding into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a bar extruder, drying at 120 ℃ for 3 hours, and roasting at 600 ℃ for 4 hours to obtain a catalyst carrier Z1.

Taking 1100 g of carrier Z, and respectively containing MoO in 82 ml₃182.9 g/L and NiO 36.6 g/L of mixed solution of ammonium heptamolybdate and nickel nitrate are dipped for 3 hours, dried for 2 hours at 120 ℃ and then roasted for 3 hours at 450 ℃ to obtain the catalyst C1.

The composition of catalyst C1 after calcination, based on the catalyst, is shown in Table 2.

Example 2

Weighing 128.6 g of pseudo-boehmite (a catalyst Changling division company) with a dry basis of 70 percent and 135.8 g of molecular sieve Y-2 (prepared by preparation example 2) with a dry basis of 81 percent, uniformly mixing, extruding into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a strip extruding machine, drying for 3 hours at 120 ℃, and roasting for 4 hours at 600 ℃ to obtain a catalyst carrier Z2.

Taking 2100 g of carrier Z, and respectively using 83 ml of carrier containing MoO₃Soaking the mixed solution of ammonium heptamolybdate and nickel nitrate with the concentration of 180.7 g/L and NiO of 36.1 g/L for 3 hours, drying the mixed solution at the temperature of 120 ℃ for 2 hours, and then roasting the dried mixed solution at the temperature of 450 ℃ for 3 hours to obtain the catalyst C2.

The composition of catalyst C2 after calcination, based on the catalyst, is shown in Table 2.

Example 3

Weighing 128.6 g of pseudo-boehmite (a catalyst Changling division company) with a dry basis of 70 percent and 132.5 g of molecular sieve Y-3 (prepared by preparation example 3) with a dry basis of 83 percent, uniformly mixing, extruding into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a strip extruding machine, drying for 3 hours at 120 ℃, and roasting for 4 hours at 600 ℃ to obtain a catalyst carrier Z3.

The carrier Z3100 g is taken, 83 ml of the carrier respectively containing MoO₃Soaking the mixed solution of ammonium heptamolybdate and nickel nitrate with the concentration of 180.7 g/L and NiO of 36.1 g/L for 3 hours, drying the mixed solution at the temperature of 120 ℃ for 2 hours, and then roasting the dried mixed solution at the temperature of 450 ℃ for 3 hours to obtain the catalyst C3.

The composition of catalyst C3 after calcination, based on the catalyst, is shown in Table 2.

Example 4

Weighing 128.6 g of pseudo-boehmite (a catalyst Changling division company) with a dry basis of 70 percent and 129.4 g of molecular sieve Y-4 (prepared by preparation example 4) with a dry basis of 85 percent, uniformly mixing, extruding into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a strip extruding machine, drying for 3 hours at 120 ℃, and roasting for 4 hours at 600 ℃ to obtain a catalyst carrier Z4.

Taking 4100 g of vector Z, and using 85 ml of vector Z containing MoO₃176.5 g/L and NiO 35.3 g/L of ammonium heptamolybdate and nickel nitrate mixed solution are soaked for 3 hours, dried at 120 ℃ for 2 hours and then roasted at 450 ℃ for 3 hours to obtain the catalyst C4.

The composition of catalyst C4 after calcination, based on the catalyst, is shown in Table 2.

Example 5

Taking 4100 g of vector Z, and using 85 ml of vector Z containing MoO₃352.9 g/L and NiO 70.6 g/L mixed solution of ammonium heptamolybdate and nickel nitrate is dipped for 3 hours, dried for 2 hours at 120 ℃ and roasted for 3 hours at 450 ℃ to obtainCatalyst C5.

The composition of catalyst C5 after calcination, based on the catalyst, is shown in Table 2.

Example 6

Taking 4100 g of vector Z, and using 85 ml of vector Z containing MoO₃176.5 g/l of a mixed solution of ammonium heptamolybdate and cobalt nitrate with 35.3 g/l of CoO was immersed for 3 hours, dried at 120 ℃ for 2 hours and then calcined at 450 ℃ for 3 hours to obtain catalyst C6.

The composition of catalyst C6 after calcination, based on the catalyst, is shown in Table 2.

Example 7

Taking 4100 g of vector Z, using 85 ml to respectively contain WO₃258.8 g/L and NiO 35.3 g/L of mixed solution of ammonium metatungstate and nickel nitrate are soaked for 3 hours, and after being dried for 2 hours at the temperature of 120 ℃, the mixed solution is roasted for 3 hours at the temperature of 450 ℃ to obtain the catalyst C7.

The composition of catalyst C7 after calcination, based on the catalyst, is shown in Table 2.

Example 8

185.7 g of pseudoboehmite (manufactured by catalyst Changling division) with a dry basis of 70% and 82.4 g of molecular sieve Y-4 (manufactured by preparation example 4) with a dry basis of 85% are weighed and mixed uniformly, extruded into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a bar extruder, dried for 3 hours at 120 ℃, and calcined for 4 hours at 600 ℃ to obtain the catalyst carrier Z5.

The carrier Z5100 g is taken, 82 ml of the carrier respectively contains MoO₃182.9 g/L and NiO 36.6 g/L of mixed solution of ammonium heptamolybdate and nickel nitrate are dipped for 3 hours, dried for 2 hours at 120 ℃ and then roasted for 3 hours at 450 ℃ to obtain the catalyst C8.

The composition of catalyst C8 after calcination, based on the catalyst, is shown in Table 2.

Example 9

42.9 g of pseudo-boehmite (a catalyst obtained from Long Ling division) with a dry basis of 70% and 200.0 g of molecular sieve Y-4 (prepared from preparation example 4) with a dry basis of 85% are weighed and mixed uniformly, extruded into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on a bar extruder, dried at 120 ℃ for 3 hours, and calcined at 600 ℃ for 4 hours to obtain a catalyst carrier Z6.

Take carrier Z6100 g, use87 ml of MoO₃172.4 g/L of NiO 34.5 g/L of ammonium heptamolybdate and nickel nitrate mixed solution is soaked for 3 hours, dried at 120 ℃ for 2 hours and then roasted at 450 ℃ for 3 hours to obtain the catalyst C9.

The composition of catalyst C9 after calcination, based on the catalyst, is shown in Table 2.

Example 10

42.9 g of pseudo-boehmite (a catalyst, Changling division company) with a dry basis of 70%, 117.6 g of molecular sieve Y-4 (prepared by preparation example 4) with a dry basis of 85% and 92.1 g of silica-alumina (Sasol company, Germany) with a dry basis of 76% are weighed and mixed uniformly, extruded into a three-blade bar shape with a circumscribed circle diameter of 1.6 mm on a bar extruder, dried for 3 hours at 120 ℃, and calcined for 4 hours at 600 ℃ to obtain a catalyst carrier Z7.

Taking Z7100 g of carrier, and respectively containing 88 ml of MoO₃170.5 g/L and 34.1 g/L NiO of ammonium heptamolybdate and nickel nitrate mixed solution are soaked for 3 hours, dried at 120 ℃ for 2 hours and then roasted at 450 ℃ for 3 hours to obtain the catalyst C10.

The composition of catalyst C10 after calcination, based on the catalyst, is shown in Table 2.

Comparative example 1

Weighing 128.6 g of pseudo-boehmite (catalyst Changling division) with a dry basis of 70% and 144.7 g of the existing Y molecular sieve (marked as D-1, catalyst Changling division, commercial trade mark LAY, the property of which is shown in Table 1) with a dry basis of 76%, uniformly mixing, extruding into a three-blade bar shape with the circumscribed circle diameter of 1.6 mm on an extruding machine, drying for 3 hours at 120 ℃, and roasting for 4 hours at 600 ℃ to obtain a catalyst carrier D.

Taking 100 g of carrier D and using 77 ml of carrier D containing MoO respectively₃194.8 g/l and 39.0 g/l NiO of ammonium heptamolybdate and nickel nitrate mixed solution, soaking for 3 hours, drying at 120 ℃ for 2 hours, and then roasting at 450 ℃ for 3 hours to obtain the catalyst D1.

The composition of catalyst D after calcination, based on the catalyst, is shown in Table 2.

TABLE 2 compositions of catalysts in examples 1-10 and comparative examples

The performance of the hydrocracking catalyst provided by the present invention was tested by the following application examples.

Application example 1

With a density of 0.9861 g/cm³The performance of the catalyst C1 provided by the invention was evaluated on a 30 ml fixed bed apparatus using a catalytic cracking diesel fuel with a sulfur content of 11000ppm, a nitrogen content of 812ppm and a total aromatic content of 88.6% as a raw material, wherein the upper part of the bed was filled with an industrial refined catalyst, the lower part was filled with a catalyst C1, and the loading of the catalyst C1 was 15 ml.

Pre-vulcanizing catalyst C1 before feeding raw oil, wherein the vulcanization conditions are as follows: 2 hours at 110 ℃ and 4 hours at 300 ℃, and the vulcanized oil is kerosene containing 6 weight percent of carbon disulfide.

Reaction conditions in the hydrofining reaction zone: the reaction temperature is 370 ℃, the hydrogen partial pressure is 6.5MPa, and the liquid hourly space velocity is 1.5h^-1Hydrogen-oil volume ratio 1000 and reaction conditions in the hydrocracking reaction zone: the reaction temperature is 400 ℃, the hydrogen partial pressure is 6.5MPa, and the liquid hourly space velocity is 1.0 hour^-1Hydrogen-oil volume ratio 1000.

The test results are listed in table 3.

Application example 2

The performance of catalyst C2 was tested under the same conditions as in application example 1, and the test results are shown in Table 3.

Application example 3

The performance of catalyst C3 was tested under the same conditions as in application example 1, and the test results are shown in Table 3.

Application example 4

The performance of catalyst C4 was tested under the same conditions as in application example 1, and the test results are shown in Table 3.

Comparative application example 1

The catalyst D1 was tested for performance under the same conditions and with the same feed as in application example 1, and the test results are shown in Table 3.

TABLE 3 catalyst reaction Performance

The test results in table 3 show that, compared with the existing catalyst, the catalyst provided by the invention can obtain higher gasoline yield and higher heavy naphtha selectivity when being used for catalyzing the hydrocracking process of diesel oil and keeping higher gasoline octane number. When the stability of the catalyst is rapidly measured in a temperature return mode, the catalyst provided by the invention is found to have lower temperature loss compared with the existing catalyst, namely the catalyst provided by the invention also has higher activity stability.

It should be noted by those skilled in the art that the described embodiments of the present invention are merely exemplary and that various other substitutions, alterations, and modifications may be made within the scope of the present invention. Accordingly, the present invention is not limited to the above-described embodiments, but is only limited by the claims.