CN109718835B

CN109718835B - Hydrocracking catalyst, preparation method and application thereof

Info

Publication number: CN109718835B
Application number: CN201711046503.2A
Authority: CN
Inventors: 毛以朝; 李明丰; 张润强; 赵阳; 赵广乐
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: 2017-10-31
Filing date: 2017-10-31
Publication date: 2021-03-12
Anticipated expiration: 2037-10-31
Also published as: CN109718835A

Abstract

The present disclosure relates to a hydrocracking catalyst, a preparation method and an application thereof, wherein the catalyst comprises a carrier of 45-90 wt% calculated by dry weight of the catalyst, a first metal component of 1-40 wt% calculated by metal oxide, and a second metal component of 1-15 wt% calculated by metal oxide; the carrier comprises a phosphorus-containing Y-type molecular sieve, weakly acidic silicon aluminum and aluminum oxide, wherein the weight ratio of the phosphorus-containing Y-type molecular sieve to the weakly acidic silicon aluminum to the aluminum oxide is 1: (0.03-20): (0.03-20); the first metal is a metal selected from group VIB; the second metal component is a metal selected from group VIII; calculated by oxide, the phosphorus content of the phosphorus-containing Y-type molecular sieve is 0.3-5 wt%, the pore volume is 0.2-0.95 mL/g, and the ratio of pyridine infrared B acid to pyridine infrared L acid is 2-10. The catalyst has high hydrocracking reaction activity.

Description

Hydrocracking catalyst, preparation method and application thereof

Technical Field

The disclosure relates to a hydrocracking catalyst, a preparation method and an application thereof.

Background

The industrial hydrocracking feed comprises 350-540 ℃ fractions such as VGO and the like, and contains a large amount of polycyclic aromatic hydrocarbons and cycloparaffins, and researches show that in a hydrocracking high-conversion-rate area, the content of the aromatic hydrocarbons in the heavy fraction is reduced, and the content of the cycloparaffins is high, so that the ring opening performance becomes an effective means for improving the quality of tail oil and increasing the smoke point of aviation kerosene. However, since the beta bond in the cycloalkane is in the vertical direction of the empty p orbital of the cycloalkane carbonium ion, so that the two are not easily formed into a coplanar conformation, this makes the cycloalkane ring-opening require stronger acidity. The molecular sieve has high acidity and is widely applied to hydrocracking reaction. However, the common HY molecular sieve has an unstable structure, framework dealumination is easy to occur in the catalyst preparation and use processes, non-framework aluminum generated in the molecular sieve preparation process is generally weak in acid, a B acid center is shielded, and the catalyst performance is reduced. The molecular sieve structure can be stabilized by performing the ultra-stabilization treatment in the modes of hydrothermal treatment, introduction of a second component and the like. The second component introduced therein generally comprises an olefinic component and a phosphorus component. As phosphorus and non-framework aluminum removed from the molecular sieve form a phosphorus-aluminum oxide complex with larger molecular weight in the roasting process, the complex has higher thermal stability and is beneficial to preventing framework dealumination, so that the complex can replace the function of rare earth components to a certain extent.

Patent CN1279130A discloses a process for preparing a phosphorus-containing Y-type molecular sieve, which comprises mixing a phosphorus-containing Y-type molecular sieve containing 0.5-5 wt% (as P)₂O₅Calculated) phosphorus, Na₂P-NH with O content of 0.5-6 wt% and unit cell constant of 2.460-2.475 nm₄Carrying out hydrothermal roasting on the NaY molecular sieve for 0.5-4 hours at 450-700 ℃ in a roasting furnace in an atmosphere of 100% water vapor; carrying out liquid-phase aluminum extraction and silicon supplement reaction on the roasted product; then filtered and washed. The obtained phosphorus-containing ultrastable Y-type molecular sieve has good product selectivity, hydrothermal stability and good vanadium poisoning resistance, and when the cracking catalyst containing the molecular sieve is used for hydrocarbon cracking reaction, the yield of light oil is high, the yield of coke is low, the conversion capacity of heavy oil is high, and the olefin content in gasoline is low.

Patent ZL200410071122.6 discloses a phosphorus-containing molecular sieve containing 85-99.9 wt% of molecular sieve and P₂O₅0.1 to 15% by weight of phosphorus, based on the weight of the molecular sieve³¹In the P MAS-NMR spectrum, the percentage of the peak area of the peak with the chemical shift of 0 +/-1.0 ppm in the total peak area is less than 1%. The preparation method of the molecular sieve comprises the steps of introducing phosphorus into the molecular sieve and using acid-containing water solutionWashing the molecular sieve with water, wherein the acid is selected from one or more of water-soluble organic acid and inorganic acid, the acid content is 0.0001-10.0 mol/L, and the washing temperature is room temperature-95 deg.C. The invention is characterized in that after the introduction of phosphorus, the method comprises a step of washing the molecular sieve by an acid solution, and the hydrocracking catalyst prepared by the phosphorus-containing molecular sieve has higher hydrocracking activity while maintaining high selectivity.

The prior art generally post-treats phosphorus-containing molecular sieves to further improve the stability and acidity of the molecular sieves. These post-treatment methods typically comprise heat treatment and acid treatment. In general, the introduction mode of water in the hydrothermal treatment process comprises two modes, namely, water vapor is introduced in the roasting process, and the material is self-heated and roasted to release water. In the two modes, as the water vapor pressure is increased sharply along with the rise of the temperature, in order to enable the existing equipment to bear the requirement of the reaction pressure, an open system is usually adopted, so that the powder is continuously taken out of the system along with the water vapor in the hydrothermal process, the reaction system is in unsteady operation, the product quality is not high, and the obtained molecular sieve has certain open-loop activity but still cannot meet the actual requirement.

Disclosure of Invention

The purpose of the disclosure is to provide a hydrocracking catalyst, a preparation method and an application thereof, wherein the catalyst has higher hydrocracking reaction activity.

To achieve the above object, a first aspect of the present disclosure: providing a hydrocracking catalyst, wherein the hydrocracking catalyst comprises 45-90 wt% of a carrier, 1-40 wt% of a first metal component and 1-15 wt% of a second metal component, wherein the carrier is calculated by the weight of the carrier on a dry basis, the first metal component is calculated by metal oxide, and the second metal component is calculated by the weight of the metal oxide;

the carrier comprises a phosphorus-containing Y-type molecular sieve, weakly acidic silicon aluminum and aluminum oxide, wherein the weight ratio of the phosphorus-containing Y-type molecular sieve to the weakly acidic silicon aluminum to the aluminum oxide is 1: (0.03-20): (0.03-20); the first metal is a metal selected from group VIB; the second metal component is a metal selected from group VIII;

calculated by oxide, the phosphorus content of the phosphorus-containing Y-type molecular sieve is 0.3-5 wt%, the pore volume is 0.2-0.95 mL/g, and the ratio of pyridine infrared B acid to pyridine infrared L acid is 2-10.

Optionally, the catalyst comprises 55 to 85 wt% of a carrier, 12 to 35 wt% of a first metal component, and 2 to 10 wt% of a second metal component, based on the dry weight of the catalyst;

the weight ratio of the phosphorus-containing Y-type molecular sieve to the weakly acidic silicon aluminum to the aluminum oxide is 1: (0.1-15): (0.1-15).

Alternatively, Al of the phosphorus-containing Y-type molecular sieve²⁷In NMR structural spectrum, I_60ppm/I_-1ppmIs 5 to 40, I_-1ppm/I_±6ppm0.4 to 2.

Optionally, the phosphorus-containing Y-type molecular sieve is prepared by a method comprising the following steps:

a. carrying out hydro-thermal treatment on a phosphorus-containing molecular sieve raw material for 0.5-10h at the temperature of 350-700 ℃ and the pressure of 0.1-2MPa in the presence of water vapor to obtain a hydro-thermally treated molecular sieve material; calculated by oxide and based on the dry weight of the phosphorus-containing molecular sieve raw material, the phosphorus content of the phosphorus-containing molecular sieve raw material is 0.1-15 wt%, and the sodium content is 0.5-4.5 wt%;

b. b, adding water into the molecular sieve material subjected to the hydrothermal treatment obtained in the step a for pulping to obtain molecular sieve slurry, heating the molecular sieve slurry to 40-95 ℃, keeping the temperature, and continuously adding an acid solution into the molecular sieve slurry, wherein the ratio of the weight of acid in the acid solution to the dry weight of the phosphorus-containing molecular sieve raw material is (0.01-0.6): 1, based on 1L of the molecular sieve slurry, taking H as reference⁺And (3) the adding speed of the acid solution is 0.05-10 mol/h, the constant temperature reaction is carried out for 0.5-20h after the acid is added, and a solid product is collected.

Optionally, in the step a, the phosphorus-containing molecular sieve is a phosphorus-containing Y-type molecular sieve, the unit cell constant of the phosphorus-containing Y-type molecular sieve is 2.425-2.47 nm, and the specific surface area is 250-750 m²The pore volume is 0.2 to 0.95 ml/g.

Optionally, in the step a, the water content of the phosphorus-containing molecular sieve raw material is 10-40 wt%;

the phosphorus-containing molecular sieve raw material is granular, the content of the phosphorus-containing molecular sieve raw material with the granularity range of 1 mm-500 mm is 10-100 wt% of the total weight of the phosphorus-containing molecular sieve raw material, and the granularity is calculated by the diameter of a circumscribed circle of the granules.

Optionally, the content of the phosphorus-containing molecular sieve raw material with the particle size range of 1 mm-500 mm is 30-100 wt% of the total weight of the phosphorus-containing molecular sieve raw material;

preferably, the content of the phosphorus-containing molecular sieve raw material with the particle size range of 5 mm-100 mm is 30-100 wt% of the total weight of the phosphorus-containing molecular sieve raw material.

Optionally, in step b, the ratio of the weight of water in the molecular sieve slurry obtained after pulping to the dry weight of the phosphorus-containing molecular sieve raw material is (14-5): 1.

optionally, the preparation step of the phosphorus-containing Y-type molecular sieve further comprises: in the step b, adding ammonium salt into the molecular sieve slurry in the process of adding the acid solution, wherein the ammonium salt is at least one selected from ammonium nitrate, ammonium chloride and ammonium sulfate, and the weight ratio of the ammonium salt to the dry basis weight of the phosphorus-containing molecular sieve raw material is (0.1-2.0): 1.

optionally, in the step b, the acid concentration of the acid solution is 0.01-15.0 mol/L, and the acid is at least one selected from phosphoric acid, sulfuric acid, nitric acid, hydrochloric acid, acetic acid, citric acid, tartaric acid, formic acid and acetic acid.

Optionally, the preparation step of the phosphorus-containing Y-type molecular sieve further comprises: collecting the solid product, then washing with water and drying to obtain a phosphorus-containing molecular sieve; the drying conditions are as follows: the temperature is 50-350 ℃, and preferably 70-200 ℃; the time is 1-24 h, preferably 2-6 h.

Optionally, the acidity value of the infrared B acid of the weakly acidic silicon aluminum is 0.01-0.1 mmol/g, the silicon content is 20-60 wt% in terms of silicon dioxide, and the pore volume is 0.5-1.0 ml/g; the weakly acidic silicon-aluminum is silicon-containing aluminum oxide and/or amorphous silicon-aluminum.

Optionally, the first metal is molybdenum and/or tungsten; the second metal is at least one selected from iron, nickel and cobalt.

A third aspect of the disclosure: there is provided a process for preparing a hydrocracking catalyst according to the first aspect of the present disclosure, the process comprising: the impregnation liquid containing the metal precursor is contacted with the carrier for impregnation, and then the material obtained after the impregnation is dried.

Optionally, the method further comprises: mixing a phosphorus-containing Y-type molecular sieve, alumina, weakly acidic silicon aluminum, a peptizing agent and an optional lubricant, and then molding, drying and roasting to obtain the carrier.

Optionally, the metal precursor comprises a first metal precursor and a second metal precursor, wherein the first metal precursor is at least one selected from inorganic acids of the first metal, inorganic salts of the first metal, and first metal organic compounds; the inorganic salt is at least one selected from nitrate, carbonate, basic carbonate, hypophosphite, phosphate, sulfate and chloride; the organic substituent in the first metal organic compound is at least one selected from hydroxyl, carboxyl, amino, ketone, ether and alkyl;

the second metal precursor is at least one selected from inorganic acid of a second metal, inorganic salt of the second metal and a second metal organic compound; the inorganic salt is at least one selected from nitrate, carbonate, basic carbonate, hypophosphite, phosphate, sulfate and chloride; the organic substituent in the second metal organic compound is at least one selected from hydroxyl, carboxyl, amino, ketone, ether and alkyl.

Optionally, the impregnation liquid further contains an organic additive; the concentration of the organic additive is 2-300 g/L; the organic additive is at least one selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid, 1, 2-cyclohexanediamine tetraacetic acid, citric acid, tartaric acid, malic acid, ethylenediamine, diethylenetriamine, cyclohexanediamine tetraacetic acid, glycine, nitrilotriacetic acid, ethylenediaminetetraacetic acid, and ammonium ethylenediaminetetraacetate.

Optionally, the drying conditions are: the temperature is 80-350 ℃, and the time is 0.5-24 hours.

Optionally, the method further comprises a step of drying the contacted material and then roasting, wherein roasting conditions are as follows: the temperature is 350-600 ℃, and the time is 0.2-12 hours.

A third aspect of the disclosure: there is provided the use of a hydrocracking catalyst according to the first aspect of the present disclosure in a hydrocracking reaction of a hydrocarbon feedstock.

Optionally, the hydrocarbon feedstock is at least one selected from the group consisting of straight run gas oil, vacuum gas oil, demetallized oil, atmospheric residue, deasphalted vacuum residue, coker distillate, catalytically cracked distillate, shale oil, tar sand oil, and coal liquefaction oil;

the conditions of the hydrocracking reaction are as follows: the reaction temperature is 200-650 ℃, preferably 300-510 ℃; the reaction pressure is 3-24 MPa, preferably 4-15 MPa; the liquid hourly space velocity is 0.1-10 hours^-1Preferably 0.2 to 5 hours^-1(ii) a The volume ratio of hydrogen to oil is 100-5000, preferably 200-1000.

According to the technical scheme, the phosphorus-containing molecular sieve raw material is subjected to special hydrothermal treatment and acid washing treatment to prepare the phosphorus-containing molecular sieve with excellent performance, the ratio of the acid content of B to the acid content of L is further improved, and the hydrocracking catalyst prepared from the phosphorus-containing molecular sieve has higher hydrocracking activity and ring opening selectivity.

Additional features and advantages of the disclosure will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:

FIG. 1 is Al of molecular sieves prepared in preparation examples 1 to 3 and comparative examples 1 to 4²⁷-NMR structural spectrum.

Detailed Description

The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.

The first aspect of the disclosure: providing a hydrocracking catalyst, wherein the hydrocracking catalyst comprises 45-90 wt% of a carrier, 1-40 wt% of a first metal component and 1-15 wt% of a second metal component, wherein the carrier is calculated by the weight of the carrier on a dry basis, the first metal component is calculated by metal oxide, and the second metal component is calculated by the weight of the metal oxide; preferably, the catalyst comprises 55 to 85 wt% of the carrier, 12 to 35 wt% of the first metal component, and 2 to 10 wt% of the second metal component, on a dry basis, based on the weight of the catalyst on a dry basis, on a metal oxide basis. The carrier comprises a phosphorus-containing Y-type molecular sieve, weakly acidic silicon aluminum and aluminum oxide, wherein the weight ratio of the phosphorus-containing Y-type molecular sieve to the weakly acidic silicon aluminum to the aluminum oxide is 1: (0.03-20): (0.03-20), preferably 1: (0.1-15): (0.1-15). The first metal is a metal selected from group VIB; the second metal component is a metal selected from group VIII.

In the hydrocracking catalyst disclosed by the disclosure, the phosphorus-containing Y-type molecular sieve as a carrier component has special performance, so that the hydrocracking catalyst has higher hydrocracking activity and ring-opening selectivity. Calculated by oxide, the phosphorus content of the phosphorus-containing Y-type molecular sieve is 0.3-5 wt%, the pore volume is 0.2-0.95 mL/g, and the ratio of pyridine infrared B acid to pyridine infrared L acid is 2-10.

The phosphorus-containing Y-type molecular sieve has a higher ratio of the B acid content to the L acid content. Particularly, the phosphorus-containing Y-type molecular sieve not only reserves high ratio of framework aluminum to non-framework aluminum, but also reserves certain non-framework aluminum at a position of-4 to-6 ppm or at a position of 3 to 7ppm at the position of the non-framework aluminum. In particular, Al of the molecular sieve²⁷In the NMR structural spectrum, the peak height ratio of the skeletal aluminum to the non-skeletal aluminum, i.e., I, is at 60. + -.1 ppm and-1. + -.1 ppm_60ppm/I_-1ppm5 to 40; and the chemical shift position of 0ppm of non-framework aluminum has two obvious characteristic peaks: -1. + -.1 ppm, and-5.5. + -.2 ppm or 3 to 7ppm, both peak heightsRatio i.e. I_-1ppm/I_±6ppm0.4 to 2, preferably 0.8 to 2, wherein I_±6ppmTaking the larger value of peak height of-5.5 +/-2 ppm and 3-7 ppm.

The phosphorus-containing Y-type molecular sieve is prepared by carrying out special hydrothermal treatment and acid washing treatment on a phosphorus-containing molecular sieve raw material. Specifically, the phosphorus-containing Y-type molecular sieve is prepared by a method comprising the following steps:

According to the present disclosure, in step a, the phosphorus-containing molecular sieve raw material refers to a phosphorus-containing molecular sieve. By adopting the phosphorus-containing molecular sieve as a raw material, the phosphorus-aluminum species outside the molecular sieve framework can improve the framework stability of the molecular sieve, thereby further improving the performance of the molecular sieve. The structure of the phosphorus-containing molecular sieve raw material can be an octahedral zeolite molecular sieve structure, preferably a phosphorus-containing Y-type molecular sieve, the unit cell constant of the phosphorus-containing molecular sieve raw material can be 2.425-2.47 nm, and the specific surface area of the phosphorus-containing molecular sieve raw material can be 250-750 m²The pore volume may be 0.2 to 0.95 ml/g. Further, the specific selection of the Y-type molecular sieve may be widely varied as long as the phosphorus-containing molecular sieve raw material satisfies the above conditions, and for example, the Y-type molecular sieve may be selected from NaY, HNaY (hydrogen Y-type molecular sieve), REY (rare earth Y-type molecular sieve), USY (ultrastable Y-type molecular sieve)) And the like. The cation position of the phosphorus-containing Y-type molecular sieve can be occupied by one or more of sodium ions, ammonium ions and hydrogen ions; alternatively, the sodium, ammonium, and hydrogen ions may be replaced by other ions, either before or after the molecular sieve is introduced with phosphorus, by conventional ion exchange. The phosphorus-containing molecular sieve raw material can be a commercial product, and can also be prepared by any prior art, for example, a method for preparing USY disclosed in a patent ZL00123139.1, or a method for preparing PUSY disclosed in a patent ZL200410071122.6 and the like can be adopted, and the details of the disclosure are not repeated.

According to the disclosure, in the step a, the water content of the phosphorus-containing molecular sieve raw material is preferably 10 to 40 wt%. The phosphorus-containing molecular sieve raw material with the water content can be obtained by adding water into the molecular sieve, pulping, filtering and drying. The phosphorus-containing molecular sieve raw material is preferably granular, and the content of the phosphorus-containing molecular sieve raw material with the granularity range of 1 mm-500 mm can be 10-100 wt%, preferably 30-100 wt% of the total weight of the phosphorus-containing molecular sieve raw material. Further, the content of the phosphorus-containing molecular sieve raw material with the granularity range of 5 mm-100 mm is 30-100 wt% of the total weight of the phosphorus-containing molecular sieve raw material. Wherein the particle size is in terms of the diameter of the circumscribed circle of particles. The adoption of the phosphorus-containing molecular sieve raw material with the granularity range for hydrothermal treatment can obviously improve the mass transfer effect of the hydrothermal treatment, reduce the material loss and improve the stability of operation. The particle size control method of the molecular sieve raw material can be conventional in the field, such as a sieving method, an extrusion strip method, a rolling ball method and the like.

According to the present disclosure, the meaning of the water-adding beating in step b is well known to those skilled in the art, and the ratio of the weight of water in the molecular sieve slurry obtained after beating to the dry weight of the phosphorus-containing molecular sieve raw material can be (14-5): 1.

according to the present disclosure, in the step b, the molecular sieve slurry is preferably heated to 50-85 ℃, and then the temperature is maintained and the acid solution is continuously added to the molecular sieve slurry until the weight of the acid in the added acid solution reaches a set amount. The most important of the preparation steps of the phosphorus-containing Y-type molecular sieve is that a continuous acid adding mode is adopted, acid adding and acid washing reaction are carried out simultaneously, the acid adding speed is low, the dealumination process is more moderate, and the improvement of the performance of the molecular sieve is facilitated.

According to the present disclosure, the acid solution may be continuously added to the molecular sieve slurry at one time, that is, the whole acid solution is continuously added according to a specific acid adding speed, and then the reaction is performed at a constant temperature. In particular, the acid solution may also be added in multiple portions in order to increase the utilization of the material and reduce the waste output. For example, the acid solution can be added to the molecular sieve slurry at a specific acid addition rate of 2-10 times, and after each acid addition, the reaction can be carried out at constant temperature for a period of time to continue the next acid addition until the set amount of the acid solution is added. When the acid solution is added in multiple portions, the ratio of the weight of acid in the acid solution to the dry weight of the phosphorus-containing molecular sieve starting material is preferably (0.01-0.3): 1. the acid concentration of the acid solution can be 0.01-15.0 mol/L, and the pH value can be 0.01-3. The acid may be a conventional inorganic acid and/or organic or acid, and for example, may be at least one selected from phosphoric acid, sulfuric acid, nitric acid, hydrochloric acid, acetic acid, citric acid, tartaric acid, formic acid and acetic acid.

According to the present disclosure, the preparation step of the phosphorus-containing Y-type molecular sieve may further include: in step b, adding an ammonium salt into the molecular sieve slurry during the adding of the acid solution, wherein the ammonium salt can be at least one selected from ammonium nitrate, ammonium chloride and ammonium sulfate, and the weight ratio of the ammonium salt to the dry weight of the phosphorus-containing molecular sieve raw material can be (0.1-2.0): 1. the ammonium salt may be added to the molecular sieve slurry independently of the acid solution, or an aqueous solution containing the ammonium salt and the acid may be prepared in a desired amount and added to the molecular sieve slurry.

According to the present disclosure, the preparation step of the phosphorus-containing Y-type molecular sieve may further include: and collecting the solid product, and then washing and drying to obtain the phosphorus-containing Y-type molecular sieve. The washing and drying are conventional steps for preparing the molecular sieve, and the disclosure is not particularly limited. For example, the drying may be performed by using an oven, a mesh belt, a converter, or the like, and the drying conditions may be: the temperature is 50-350 ℃, and preferably 70-200 ℃; the time is 1-24 h, preferably 2-6 h.

In accordance with the present disclosure, the alumina may include gibbsite such as gibbsite, bayerite nordstrandite, and diaspore such as boehmite (boehmite, diasporite, pseudoboehmite). The source of alumina is not particularly limited in this disclosure provided that it sufficiently meets the requirements of the present disclosure, and for example, it may be commercially available or prepared by any conventional method, such as pseudo-boehmite prepared by aluminum sulfate and sodium metaaluminate neutralization method disclosed in patent CN 100999328B.

According to the disclosure, the acidity value of the infrared B acid of the weakly acidic silicon aluminum can be 0.01 to 0.1mmol/g, the silicon content of the weakly acidic silicon aluminum as a reference and calculated by silicon dioxide can be 20 to 60 wt%, and the pore volume can be 0.5 to 1.0 ml/g. The weakly acidic silicon aluminum is, for example, silicon-containing alumina and/or amorphous silicon aluminum. The present disclosure is not particularly limited with respect to the source of the weakly acidic silica-alumina.

According to the present disclosure, preferably, the first metal is molybdenum and/or tungsten; the second metal is at least one selected from iron, nickel and cobalt.

In a second aspect of the present disclosure: there is provided a process for preparing a hydrocracking catalyst according to the first aspect of the present disclosure, the process comprising: the impregnation liquid containing the metal precursor is contacted with the carrier for impregnation, and then the material obtained after the impregnation is dried. The contact impregnation method of the impregnation liquid and the carrier can adopt any one of the methods known in the art, for example, the method disclosed in patent CN200810241082.3, which comprises loading a group VIB metal component, a group VIII metal component and an organic additive onto a catalyst carrier, wherein the process of loading the group VIB metal component, the group VIII metal component and the organic additive onto the catalyst carrier is any one of the following methods:

mode 1: contacting the catalyst carrier with a first solution, then contacting with a second solution, or contacting the catalyst carrier with a second solution, then contacting with the first solution, wherein the first solution contains a compound of a group VIB metal component and a compound of a group VIII metal component, the second solution contains a compound of a group VIB metal component but does not contain a compound of a group VIII metal component, and the first solution and/or the second solution contain the organic additive;

mode 2: contacting the catalyst carrier with a third solution and then with a fourth solution, or contacting the catalyst carrier with a fourth solution and then with a third solution, wherein the third solution contains a compound of a group VIB metal component, the fourth solution contains a compound of a group VIII metal component and an organic auxiliary agent but does not contain the compound of the group VIB metal component, and the third solution contains or does not contain the compound of the group VIII metal component and the organic additive,

wherein, after each contact, the catalyst support after the contact is heated.

Methods for preparing the carrier are well known to those skilled in the art, and the present disclosure is not particularly limited. For example, the method may further comprise: mixing a phosphorus-containing Y-type molecular sieve, alumina, weakly acidic silicon aluminum, a peptizing agent and an optional lubricant, and then molding, drying and roasting to obtain the carrier. The molding method can adopt various conventional methods, such as tabletting molding, rolling ball molding or extrusion molding. When the extrusion molding method is employed, an appropriate amount of an auxiliary is preferably added to facilitate molding.

Optionally, the preparation method of the carrier comprises: mixing a phosphorus-containing Y-type molecular sieve, alumina, weakly acidic silicon aluminum, a peptizing agent and an optional lubricant, and then molding, drying and roasting to obtain the carrier. The peptizing agent can be an acid-containing solution or an alkali-containing solution, the acid is at least one of organic acid or inorganic acid familiar to the technical field, such as at least one of phosphoric acid, sulfuric acid, nitric acid, hydrochloric acid, acetic acid, tungstic and/or molybdic heteropoly acid, citric acid, tartaric acid, formic acid and acetic acid, and ammonium, iron, cobalt, nickel, aluminum and other cations can be added into the acid-containing solution to keep the acid; the alkali-containing solution comprises at least one of ammonia, organic amine, and urea.

The shape of the carrier is not particularly required in the present disclosure, and may be spherical, strip-shaped, hollow strip-shaped, spherical, block-shaped, etc., and the strip-shaped carrier may be cloverleaf, clover, etc., and variations thereof.

In an alternative embodiment of the present disclosure, the support may be prepared as disclosed in patent CN107029779A, specifically: (1) mixing a phosphorus-containing Y-type molecular sieve, alumina, weakly acidic silicon aluminum, a peptizing agent, a lubricant and water to obtain a mixture, wherein the dosage of each component enables the weight ratio of the mass of the peptizing agent to the powder in the mixture to be 0.28 multiplied by 10^-4～4.8×10^-4mol/g, the ratio of the weight of water to the amount of mass of peptizing agent is 2.0X 10³～30×10³g/mol, wherein the weight of the powder is the sum of the weights of the phosphorus-containing Y-type molecular sieve, alumina and weakly acidic silicon aluminum, and the mass of the peptizing agent refers to the mole number of H protons metered in the peptizing agent; the lubricant is one or two of sesbania powder and graphite; (2) and (2) kneading, molding, drying and roasting the mixture obtained in the step (1) to obtain the carrier.

According to the present disclosure, the metal precursors include a first metal precursor and a second metal precursor. Wherein the first metal precursor is a soluble compound containing the first metal, and comprises at least one of an inorganic acid of the first metal, an inorganic salt of the first metal and a first metal organic compound; the inorganic salt may be at least one selected from the group consisting of nitrate, carbonate, hydroxycarbonate, hypophosphite, phosphate, sulfate and chloride; the organic substituent in the first metal organic compound is at least one selected from hydroxyl, carboxyl, amino, ketone, ether and alkyl. For example, when the first metal is molybdenum, the first metal precursor may be at least one selected from the group consisting of molybdic acid, paramolybdic acid, molybdate, paramolybdate, and the like; when the first metal is tungsten, the first metal precursor may be at least one selected from the group consisting of tungstic acid, metatungstic acid, ethyl metatungstic acid, tungstate, metatungstate, and ethyl metatungstate. The second metal precursor is a soluble compound containing the second metal and comprises at least one of inorganic acid of the second metal, inorganic salt of the second metal and organic compound of the second metal; the inorganic salt may be at least one selected from the group consisting of nitrate, carbonate, hydroxycarbonate, hypophosphite, phosphate, sulfate and chloride; the organic substituent in the second metal organic compound is at least one selected from hydroxyl, carboxyl, amino, ketone, ether and alkyl.

According to the present disclosure, the impregnation fluid may further contain an organic additive; the concentration of the organic additive may be 2-300 g/L. The organic additive is an oxygen-containing organic compound and/or a nitrogen-containing organic compound. Specifically, the oxygen-containing organic compound may be at least one selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol (molecular weight may be 200 to 1500), diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid, 1, 2-cyclohexanediaminetetraacetic acid, citric acid, tartaric acid, and malic acid; the nitrogen-containing organic compound may be at least one selected from the group consisting of ethylenediamine, diethylenetriamine, cyclohexanediaminetetraacetic acid, glycine, nitrilotriacetic acid, ethylenediaminetetraacetic acid and ammonium ethylenediaminetetraacetate.

In the method for producing a hydrocracking catalyst of the present disclosure, the contacting temperature is not particularly limited, and may be various temperatures that the impregnation solution can reach. The time for the impregnation is also not particularly limited as long as the catalyst carrier can be supported with the desired amount of the metal active component precursor. In general, the higher the impregnation temperature, the higher the concentration of the impregnation solution, and the shorter the time required to achieve the same impregnation amount (i.e., the weight difference between the catalyst support after impregnation and the catalyst support before impregnation); and vice versa. When the desired amount and conditions of impregnation are determined, one skilled in the art can readily select an appropriate impregnation time based on the teachings of the present disclosure. The present disclosure does not specifically require an impregnation method, which may be either a saturated impregnation or a supersaturated impregnation. The impregnation may be carried out under a sealed condition or in an open environment according to a conventional method in the art, and the loss of the aqueous solvent may or may not be replenished during the impregnation. Various gases, such as air, nitrogen, water vapor, etc., may be introduced during the impregnation process, or any new components may not be introduced.

In the method for preparing a hydrocracking catalyst according to the present disclosure, the drying conditions are not particularly limited, and may be various drying conditions commonly used in the art, for example: the temperature is 80-350 deg.C, preferably 100-300 deg.C, and the time is 0.5-24 hr, preferably 1-12 hr.

The method for preparing a hydrocracking catalyst according to the present disclosure may further include a step of drying the contacted material and then calcining, which is a conventional step for preparing a catalyst, and the present disclosure is not particularly limited. The conditions for the calcination may be, for example: the temperature is 350-600 ℃, preferably 400-550 ℃; the time is 0.2 to 12 hours, preferably 1 to 10 hours.

The hydrocracking catalyst provided by the disclosure can be used as various acid catalytic catalysts in catalytic cracking, hydroisomerization, alkylation, hydrocracking and other reactions, and is particularly suitable for hydrocracking hydrocarbon raw materials to produce hydrocarbon fractions with lower boiling points and lower molecular weights. Accordingly, the third aspect of the present disclosure: there is provided the use of a hydrocracking catalyst according to the first aspect of the present disclosure in a hydrocracking reaction of a hydrocarbon feedstock.

The hydrocarbon feedstock may be various heavy mineral oils or synthetic oils or their mixed distillates, such as straight run gas oil (straight run gas oil), vacuum gas oil (vacuum gas oil), demetalized oils (demetalized oils), atmospheric residues (atmospheric residues), deasphalted vacuum residues (deasphalted vacuum residues), coker distillates (coker distillates), catalytic cracker distillates (cat distillates), shale oils (shell oils), tar sand oils (tar sand oils), coal liquefied oils (coal liquids), etc. In particular, the catalyst provided by the present disclosure is particularly suitable for hydrocracking of heavy and poor distillate to produce a hydrocracking process of middle distillate with a distillation range of 149-371 ℃, especially a distillation range of 180-370 ℃.

The application of the hydrocracking catalyst provided by the present disclosure in the hydrocracking reaction of hydrocarbon raw materials preferably further comprises the step of pre-sulfurizing the hydrocracking catalyst with sulfur, hydrogen sulfide or sulfur-containing raw materials at the temperature of 140-370 ℃ in the presence of hydrogen before using the hydrocracking catalyst, wherein the pre-sulfurization can be carried out outside a reactor or in-situ in the reactor, and the pre-sulfurization can be carried out to convert the hydrocracking catalyst into a sulfide type.

The catalyst provided by the present disclosure can be used under conventional hydrocracking process conditions when used for distillate oil hydrocracking, for example, the hydrocracking reaction conditions are as follows: the reaction temperature is 200-650 ℃, the reaction pressure is 3-24 MPa, the reaction pressure is 4-15 MPa, the liquid hourly space velocity is 0.1-10 h-1, the liquid hourly space velocity is 0.2-5 h-1, and the volume ratio of hydrogen to oil is 100-5000, and the reaction pressure is 200-1000.

The hydrocracking reaction apparatus may be any reaction apparatus sufficient to allow the hydrocarbon feedstock to react with the catalyst under hydrogenation reaction conditions, and may be, for example, a fixed bed reactor, a moving bed reactor, an ebullating bed reactor or a slurry bed reactor.

The present disclosure is further illustrated by the following examples, but is not limited thereto.

The pore volume and the specific surface area of the molecular sieve are measured by a static low-temperature adsorption capacity method (by adopting a national standard GB/T5816-1995 method) by adopting an ASAP 2400 model automatic adsorption instrument of American micromeritics instruments, and the specific method comprises the following steps: vacuumizing and degassing at 250 deg.C and 1.33Pa for 4 hr, contacting with nitrogen as adsorbate at-196 deg.C, and statically reaching adsorption balance; and calculating the nitrogen adsorption amount of the adsorbent according to the difference between the nitrogen gas inflow and the nitrogen gas remaining in the gas phase after adsorption, calculating the pore size distribution by using a BJH (British Ribose) formula, and calculating the specific surface area and the pore volume by using a BET (BET) formula.

The unit cell constant is determined by an X-ray diffractometer model D5005 of Siemens Germany, and is in accordance with the method of industry standard SH/T0339-92. The experimental conditions are as follows: cu target, Ka radiation, solid detector, tube voltage 40kV, tube current 40mA, step scanning, step width of 0.02 degrees, prefabrication time of 2s and scanning range of 5-70 degrees.

The phosphorus content and the sodium content of the molecular sieve are measured by a 3271E type X-ray fluorescence spectrometer of Japan science and Motor industry Co., Ltd, and the measuring method comprises the following steps: tabletting and forming a powder sample, carrying out rhodium target, detecting the spectral line intensity of each element by a scintillation counter and a proportional counter under the laser voltage of 50kV and the laser current of 50mA, and carrying out quantitative and semi-quantitative analysis on the element content by an external standard method.

The ratio of the B acid amount to the L acid amount of the molecular sieve is measured by a Bio-Rad IFS-3000 type infrared spectrometer. The specific method comprises the following steps: the molecular sieve sample is ground and pressed into 10mg/cm²The self-supporting sheet is placed in an in-situ cell of an infrared spectrometer at 350 ℃ and 10 DEG C^-3Surface purification treatment is carried out for 2 hours under Pa vacuum degree, pyridine saturated steam is introduced after the surface purification treatment is carried out to the room temperature, after adsorption equilibrium is carried out for 15 minutes, vacuum desorption is carried out for 30 minutes at 350 ℃, and the adsorption and determination of pyridine vibration spectrum are measured after the surface purification treatment is carried out to the room temperature. The scanning range is 1400cm^-1-1700cm^-1At 1540 + -5 cm^-1The ratio of the infrared absorption of the band to the weight and area of the sample piece defines the amount of B acid [ infrared absorption per unit area, per unit mass of the sample, expressed as: AB (cm)²·g)^-1]. At 1450 + -5 cm^-1The ratio of the infrared absorption value of the band to the weight and area of the sample piece defines the L acid amount [ infrared absorption value per unit area, unit mass of the sample, expressed as: AL (cm)²·g)^-1]The value of AB/AL is defined as the ratio of the amount of B acid to the amount of L acid of the zeolite molecular sieve.

The molecular sieve adopts a Varian UNITYINOVA300M nuclear magnetic resonance instrument to perform sample analysis, wherein the resonance frequency of Al MAS is 78.162MHzs, the rotor speed is 3000Hz, the repetition delay time is 0.5s, the sampling time is 0.020s, the pulse width is 1.6 mus, the spectrum width is 54.7kHz, the data is collected at 2000 points, the cumulative frequency is 800 times, and the test temperature is room temperature.

Yield (%) of the molecular sieve is dry basis weight of the molecular sieve obtained by preparation/dry basis weight of the hydrothermal-treated molecular sieve raw material × 100%.

Preparative examples 1-3 are provided to illustrate methods of preparing phosphorus-containing molecular sieves provided by the present disclosure.

Preparation of example 1

Taking NaY molecular sieve (product of China petrochemical catalyst Chang Ling Branch, product name NaY, unit cell constant of 2.468nm, specific surface area of 680m²Per g, pore volume of 0.30ml/g, Na₂O content 13.0 wt%, Al₂O₃22 wt.%) was added 2.0mol/L of (NH)₄)₂HPO₄Pulping the aqueous solution, filtering, repeating the above process for three times, drying at 100 deg.C for 1h to obtain phosphorus-containing molecular sieve material with unit cell constant of 2.468nm and specific surface area of 590m²Per g, pore volume of 0.37ml/g, P₂O₅The content was 4.8% by weight, Na₂The O content was 3.5% by weight.

100g of the phosphorus-containing molecular sieve raw material is put into a hydrothermal treatment device, 100% of water vapor is introduced, the temperature is raised to 450 ℃, the pressure in the device is controlled to be 0.8MPa, the hydrothermal treatment is constantly carried out for 8 hours, and then the molecular sieve material after the hydrothermal treatment is taken out.

According to the weight ratio of hydrochloric acid, ammonium chloride and phosphorus-containing molecular sieve raw materials (dry basis) of 0.2: 0.4: 1 preparing 100ml of hydrochloric acid-ammonium chloride aqueous solution, wherein the concentration of hydrochloric acid in the aqueous solution is 0.05mol/L, and the concentration of ammonium chloride in the aqueous solution is 0.07 mol/L.

Taking 50g (dry basis) of the molecular sieve material subjected to the hydrothermal treatment, adding 500ml of deionized water, stirring and pulping to obtain molecular sieve slurry, and heating the molecular sieve slurry to 80 ℃. Based on 1L of molecular sieve slurry and H⁺And adding the prepared hydrochloric acid-ammonium chloride aqueous solution into the molecular sieve slurry at a constant speed for three times at a speed of 2mol/h, reacting for 4 hours at a constant temperature after each time of adding acid, filtering, and taking a filter cake to continue to add acid for the next time in the same manner. After the last time of acid addition and reaction for 4 hours, collecting the solid product, and drying at 180 ℃ for 3 hours to obtain the phosphorus-containing molecular sieve Y-1, Al of which²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

Preparation of example 2

Taking PSRY molecular sieve (product name PSRY of China petrochemical catalyst Changling Brand, Inc.), wherein the unit cell constant is 2.456nm, and the specific surface area is 620m²Per g, pore volume of 0.39ml/g, Na₂O content 2.2 wt.%, P₂O₅Content of 1.5 wt.%, Al₂O₃In an amount of18 percent by weight) of the phosphorus-containing molecular sieve, adding deionized water into the mixture for pulping, wherein the total amount of water is 1000ml, filtering, and drying at 70 ℃ for 2 hours to obtain the phosphorus-containing molecular sieve raw material with the water content of 35 percent by weight.

Crushing the phosphorus-containing molecular sieve raw material, sieving to 5-20 meshes (wherein 1-500 mm particles account for 70 wt% of the total weight of the phosphorus-containing molecular sieve raw material), placing into a hydrothermal treatment device, introducing 100% of steam, heating to 580 ℃, controlling the pressure in the device to be 0.4MPa, performing hydrothermal treatment for 2 hours constantly, and taking out the molecular sieve material after the hydrothermal treatment.

According to the weight ratio of sulfuric acid to phosphorus-containing molecular sieve raw material (dry basis) of 0.02: 1 preparing 250ml of sulfuric acid aqueous solution, wherein the concentration of sulfuric acid in the aqueous solution is 0.2 mol/L.

Taking 50g (dry basis) of the molecular sieve material subjected to the hydrothermal treatment, adding 500ml of deionized water, stirring and pulping to obtain molecular sieve slurry, and heating to 80 ℃. Based on 1L of molecular sieve slurry and H⁺Adding the prepared sulfuric acid aqueous solution into the molecular sieve slurry at a constant speed for three times at a speed of 0.5mol/h, reacting for 2 hours at a constant temperature after each time of acid addition, filtering, and taking a filter cake to continue to add acid for the next time in the same manner. After the last time of acid addition and reaction for 2 hours, collecting the solid product, and drying at 100 ℃ for 8 hours to obtain the phosphorus-containing molecular sieve Y-2, Al of which²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

Preparation of example 3

A phosphorus-containing molecular sieve was prepared according to the method of preparation example 2, except that the phosphorus-containing molecular sieve raw material was crushed, sieved to 5 to 20 mesh (wherein 5mm to 100mm particles account for 70 wt% of the total weight of the phosphorus-containing molecular sieve raw material), and then subjected to hydrothermal treatment and subsequent operations according to the method of preparation example 2, to obtain a phosphorus-containing molecular sieve Y-3, properties of which are shown in table 1.

Comparative examples 1-4 are prepared to illustrate different methods of preparing phosphorus-containing molecular sieves than are disclosed herein.

Preparation of comparative example 1

The phosphorus-containing molecular sieve of the preparation comparative example is the PSRY molecular sieve which is the same as the preparation example 2, and the preparation method can refer to the disclosure in CN1088407CThe process for preparing a phosphorus-containing zeolite comprises directly mixing a phosphorus-containing compound with a raw material zeolite in a weight ratio of 0.1 to 40, heating the mixture at 50 to 550 ℃ for at least 0.1 hour under a closed condition, washing the resulting product with deionized water until the product is free of acid ions, and recovering the phosphorus-containing zeolite. It was designated as RY-1, its Al²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

Preparation of comparative example 2

Taking phosphorus-free HY molecular sieve (product name HY, unit cell constant 2.465nm, specific surface area 580m, produced by Zhongshiedian catalyst Chang Ling division Co., Ltd.)²Per g, pore volume of 0.33ml/g, Na₂0.3 wt.% of O, Al₂O₃Content of 22 wt%) was put into a hydrothermal treatment apparatus, 100% steam was introduced, the temperature was raised to 450 ℃, the pressure in the apparatus was controlled at 0.8MPa, and the molecular sieve material after hydrothermal treatment was taken out after constant hydrothermal treatment for 8 hours.

According to the weight ratio of 0.08 of hydrochloric acid, ammonium chloride and phosphorus-containing molecular sieve raw materials: 1.5: 1 preparing 50ml of hydrochloric acid-ammonium chloride aqueous solution, wherein the concentration of hydrochloric acid in the aqueous solution is 0.1mol/L, and the concentration of ammonium chloride in the aqueous solution is 0.16 mol/L.

Taking 50g (dry basis) of the molecular sieve material subjected to the hydrothermal treatment, adding 500ml of deionized water, stirring and pulping to obtain molecular sieve slurry, and heating the molecular sieve slurry to 80 ℃. Based on 1L of molecular sieve slurry and H⁺And adding the prepared hydrochloric acid-ammonium chloride aqueous solution into the molecular sieve slurry at a constant speed for three times at a speed of 2mol/h, reacting for 4 hours at a constant temperature after each time of adding acid, filtering, and taking a filter cake to continue to add acid for the next time in the same manner. After the last time of acid addition and reaction for 4 hours, collecting the solid product, and drying at 180 ℃ for 3 hours to obtain the phosphorus-containing molecular sieve RY-2 and Al thereof²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

Preparation of comparative example 3

300g of PSRY molecular sieve (same as preparation example 2) was taken, and NH at a concentration of 0.5mol/L was added₄600ml of Cl aqueous solution is pulped by deionized water, the total amount of water is 1000ml, the temperature is heated to 90 ℃, and ammonium exchange is carried out for 3 h. Then filtering, washing with deionized waterThe filter cake was heated twice at 600 ℃ for 4h at atmospheric pressure.

According to the weight ratio of 0.5: 0.36: 1 preparing 300ml of hydrochloric acid-ammonium chloride aqueous solution, wherein the concentration of hydrochloric acid in the aqueous solution is 0.6mol/L, and the concentration of ammonium chloride in the aqueous solution is 0.3 mol/L.

Taking 50g (dry basis) of the molecular sieve material subjected to the hydrothermal treatment, adding 500ml of deionized water, stirring and pulping to obtain molecular sieve slurry, and heating the molecular sieve slurry to 80 ℃. Based on 1L of molecular sieve slurry and H⁺And adding the prepared hydrochloric acid-ammonium chloride aqueous solution into the molecular sieve slurry at a constant speed for three times at a speed of 2mol/h, reacting for 4 hours at a constant temperature after each time of adding acid, filtering, and taking a filter cake to continue to add acid for the next time in the same manner. After the last time of acid addition and reaction for 4 hours, collecting a solid product, and drying at 180 ℃ for 3 hours to obtain a phosphorus-containing molecular sieve RY-3, Al of which²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

Preparation of comparative example 4

Taking 300g of PSRY molecular sieve (same as preparation example 2), adding deionized water for pulping, wherein the total amount of water is 1000ml, filtering, and drying at 70 ℃ for 2h to obtain the phosphorus-containing molecular sieve raw material with the water content of 65%.

And (3) putting the obtained phosphorus-containing molecular sieve raw material into a hydrothermal treatment device, heating to 580 ℃, controlling the pressure in the device to be 0.4MPa, performing hydrothermal treatment for 2 hours constantly, and taking out the molecular sieve material after the hydrothermal treatment.

According to the weight ratio of 0.8: 1 preparing 500ml of sulfuric acid aqueous solution, wherein the concentration of sulfuric acid in the aqueous solution is 0.2 mol/L.

Taking 50g (dry basis) of the molecular sieve material subjected to the hydrothermal treatment, adding 500ml of deionized water, stirring and pulping to obtain molecular sieve slurry, and heating to 80 ℃. Adding the prepared sulfuric acid aqueous solution into the molecular sieve slurry for three times, wherein the acid adding mode for each time is directly pouring, then reacting for 2 hours at constant temperature, filtering, and taking the filter cake to continue to add acid for the next time according to the same mode. After the last time of acid addition and reaction for 2 hours, collecting a solid product, and drying at 100 ℃ for 8 hours to obtain the productTo phosphorus containing molecular sieves RY-4, Al thereof²⁷The NMR structural spectrum is shown in FIG. 1, and the properties are shown in Table 1.

TABLE 1

As can be seen from table 1, the phosphorus-containing molecular sieve provided by the present disclosure has a higher ratio of the amount of the B acid to the amount of the L acid, and can improve the yield of the molecular sieve under the condition of controlling the particle size range of the phosphorus-containing molecular sieve raw material.

Examples 1-3 serve to illustrate the preparation of hydrocracking catalysts provided by the present disclosure. Comparative examples 1-4 are presented to illustrate catalysts prepared using different molecular sieves than those of the present disclosure.

Example 1

222.5g of pseudo-boehmite powder PB90 (produced by Zhongpetrochemical catalyst ChangLing division, with a pore volume of 0.9ml/g and a water content of 28 wt.%), 39.5g of Y-1 molecular sieve (with a water content of 19 wt.%), 13.2g of weakly acidic silica-alumina (produced by Germany Condea, trade name Sira-40, pore volume of 0.88ml/g and specific surface 468m²The carrier CS-1 is prepared by uniformly mixing 40% of silicon dioxide by weight, 0.04mmol/g of infrared B acid acidity value and 0.76 of dry base with 9 g of sesbania powder, adding 193ml of aqueous solution containing 7.1ml of nitric acid (65-68% of nitric acid by weight in Beijing chemical reagent factory), extruding into trilobe-shaped strips with the diameter of the circumscribed circle of 1.6 mm, drying at 120 ℃, and roasting at 600 ℃ for 3 hours.

After cooling to room temperature, 100g of CS-1 carrier was immersed in 80ml of an aqueous solution containing 52 g of ammonium metatungstate (82 wt% tungsten oxide, available from mitsubao cemented carbide works, japan), 8.7 g of basic nickel carbonate (51 wt% nickel oxide, available from jiangsu slow chemical limited), and 10.5g of citric acid, and dried at 120 ℃ for 10 hours to obtain the hydrocracking catalyst prepared in this example, the composition of which is shown in table 2.

Examples 2 to 3

A catalyst was prepared as in example 1 except that the molecular sieves used were Y-2 and Y-3, respectively, and the catalyst composition is shown in Table 2.

Example 4

97.2g of pseudo boehmite powder SB (product name SB powder, dry basis content 0.72, produced by Sasol company) and 39.5gHY molecular sieve (product name HY, dry basis content 0.76, produced by Zhongpetrochemical catalyst ChangLing division company), 12.3g of Y-2 molecular sieve (water content 19 wt%), 13.2g of weakly acidic Sira-40 and 2.8g of sesbania powder are added and mixed uniformly, 240ml of aqueous solution containing 2ml of nitric acid (content 65-68 wt% in Beijing chemical reagent factory) is added and extruded into trilobal strips with the circumscribed circle diameter of 1.6 mm, the three-leaf strips are dried at 120 ℃ and roasted at 550 ℃ for 3 hours, and the carrier CS-4 is obtained.

After cooling to room temperature, 100g of the CS-4 carrier was immersed in 90ml of an aqueous solution containing 24.1 g of ammonium heptamolybdate (tianjin tetragonal chemical corporation, molybdenum oxide content 82 wt%), dried at 120 ℃ for 10 hours, immersed in 50ml of an aqueous solution containing 46.2 g of nickel nitrate (jiangsu yixing brady chemical corporation, nickel oxide content 25.6 wt%), baked at 90 ℃ for 5 hours, and baked at 420 ℃ for 3 hours, thereby obtaining the hydrocracking catalyst prepared in this example.

Example 5

42.3g of pseudo-boehmite powder PB100 (produced by Zhongpetrochemical catalyst ChangLing division, pore volume of 1.05ml/g, water content of 29 wt.%), 172.8g of Y-3 molecular sieve (water content of 19 wt.%), 40g of weakly acidic silicon aluminum Sira-40 and 10 g of sesbania powder are mixed uniformly, 120ml of aqueous solution containing 20g of urea (Beijing chemical reagent factory) is added, three-leaf strips with the diameter of the circumscribed circle of 1.6 mm are extruded, the three-leaf strips are dried at 120 ℃ and roasted at 600 ℃ for 3 hours, and the carrier CS-5 is obtained.

After cooling to room temperature, 100g of the carrier was immersed in 85ml of an aqueous solution containing 39.2 g of ammonium metatungstate (91 wt% tungsten oxide, available from Sichuan tribute cemented carbide Co., Ltd.), 20.56 g of nickel nitrate (25.6 wt% nickel oxide, available from Jiangsu Yixing brady chemical Co., Ltd.), and 0.26g of ethylene glycol, and dried at 180 ℃ for 3 hours to obtain the hydrocracking catalyst prepared in this example, the composition of which is shown in Table 2.

Comparative examples 1 to 4

A catalyst was prepared by the method of example 1 except that the molecular sieves used were RY-1, RY-2, RY-3 and RY-4, respectively.

TABLE 2

Test examples

This test example was used to test the catalytic activity of the catalysts of examples 1-5 and comparative examples 1-4 for hydrocracking reactions. Wherein, the used raw oil is the Shashuaishui vacuum gas oil, and the physicochemical properties are shown in Table 3. The reaction results are shown in Table 4.

TABLE 3

Item	Raw oil
		Density (20 ℃ C.) (g/cm)³)	0.8885
S (wt%)	16000
		N(mg/L)	352
Simulated distillation (ASTM D-2887) (° C)
		Initial boiling point	291
50% by weight	391
		90% by weight	421

In the present test example, the evaluation method of the catalyst was: the catalyst was crushed into particles of 2 to 3 mm in diameter, 20ml of the catalyst was charged into a30 ml fixed bed reactor, and before the reaction, the catalyst was first sulfurized with kerosene containing 2% by weight of carbon disulfide under a hydrogen atmosphere according to the following procedure, and then the reaction materials were switched to carry out the reaction.

And (3) vulcanization procedure: heating to 150 ℃, introducing vulcanized oil, keeping the temperature for 1h, allowing the adsorbed temperature wave to pass through two reactors, heating to 230 ℃ at the speed of 60 ℃/h, stabilizing for 2h, heating to 360 ℃ at the speed of 60 ℃/h, and stabilizing for 6 h. Replacing the raw oil, adjusting the reaction conditions below the reaction temperature, and stabilizing for at least 20 h.

Reaction conditions are as follows: at the reaction temperature of 365 ℃, the hydrogen partial pressure of 6.4MPa and the Liquid Hourly Space Velocity (LHSV) of 1h^-1The hydrocracking reaction was carried out under the condition that the hydrogen-oil ratio (volume) was 800. The results are shown in Table 3.

Conversion (%) - (% of fraction at more than 350 ℃ in the feed-fraction at more than 350 ℃ in the product oil)/amount of fraction at more than 350 ℃ in the feed X100%.

TABLE 5

Catalyst and process for preparing same	Conversion (%)
		Example 1	60.4
Example 2	64.3
		Example 3	63.5
Example 4	71.2
		Example 5	92.3
Comparative example 1	36.5
		Comparative example 2	40.8
Comparative example 3	29.8
		Comparative example 4	52.3

From table 5, it can be seen that, under the same reaction conditions, the catalytic activity of the catalyst containing the phosphorus-containing molecular sieve provided by the present disclosure is improved by 9.1 to 55.8% compared to the molecular sieve prepared by the conventional method.

The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.

It should be noted that, in the foregoing embodiments, various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various combinations that are possible in the present disclosure are not described again.

In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.

Claims

1. A hydrocracking catalyst, characterized in that the catalyst comprises 45 to 90 wt% of a carrier, 1 to 40 wt% of a first metal component calculated as a metal oxide, and 1 to 15 wt% of a second metal component calculated as a metal oxide, based on the dry weight of the catalyst;

calculated by oxide, the phosphorus content of the phosphorus-containing Y-type molecular sieve is 0.3-5 wt%, the pore volume is 0.2-0.95 mL/g, and the ratio of pyridine infrared B acid to L acid is 2-10;

al of the phosphorus-containing Y-type molecular sieve²⁷In NMR structural spectrum, I_60ppm/I_-1ppm5 to 40, the Al²⁷Two characteristic peaks at 0ppm chemical shift of the NMR structural spectrum: the chemical shift of the first characteristic peak is-1 +/-1 ppm, the chemical shift of the second characteristic peak is-5.5 +/-2 ppm or 3-7 ppm, and the peak height ratio of the first characteristic peak to the second characteristic peak is I_-1ppm/I_±6ppmSaid I is_-1ppm/I_±6ppm0.4 to 2, wherein I_±6ppmTaking the larger value of peak height of-5.5 +/-2 ppm and 3-7 ppm.

2. The catalyst of claim 1, wherein said I_-1ppm/I_±6ppm0.8 to 2.

3. The catalyst of claim 1, wherein the catalyst comprises 55 to 85 wt% of the support, 12 to 35 wt% of the first metal component, and 2 to 10 wt% of the second metal component, on a metal oxide basis, based on the dry weight of the catalyst;

4. The catalyst of any one of claims 1-3, wherein the phosphorus-containing Y-type molecular sieve is prepared by a method comprising:

5. The catalyst of claim 4, wherein in the step a, the phosphorus-containing molecular sieve raw material is a phosphorus-containing Y-type molecular sieve, the unit cell constant of the phosphorus-containing Y-type molecular sieve is 2.425-2.47 nm, and the specific surface area is 250-750 m²The pore volume is 0.2 to 0.95 mL/g.

6. The catalyst of claim 5, wherein in the step a, the water content of the phosphorus-containing molecular sieve raw material is 10-40 wt%;

7. The catalyst of claim 6, wherein the content of the phosphorus-containing molecular sieve raw material with the particle size ranging from 1mm to 500mm is 30 to 100 wt% of the total weight of the phosphorus-containing molecular sieve raw material.

8. The catalyst according to claim 6, wherein the phosphorus-containing molecular sieve raw material having a particle size ranging from 5mm to 100mm is contained in an amount of 30 to 100 wt% based on the total weight of the phosphorus-containing molecular sieve raw material.

9. The catalyst of claim 4, wherein in step b, the ratio of the weight of water in the molecular sieve slurry obtained after beating to the dry weight of the phosphorus-containing molecular sieve feedstock is (14-5): 1.

10. the catalyst of claim 4, wherein the step of preparing the phosphorus-containing Y-type molecular sieve further comprises: in the step b, adding ammonium salt into the molecular sieve slurry in the process of adding the acid solution, wherein the ammonium salt is at least one selected from ammonium nitrate, ammonium chloride and ammonium sulfate, and the weight ratio of the ammonium salt to the dry basis weight of the phosphorus-containing molecular sieve raw material is (0.1-2.0): 1.

11. the catalyst according to claim 4, wherein in the step b, the acid concentration of the acid solution is 0.01 to 15.0mol/L, and the acid is at least one selected from phosphoric acid, sulfuric acid, nitric acid, hydrochloric acid, acetic acid, citric acid, tartaric acid and formic acid.

12. The catalyst of claim 4, wherein the step of preparing the phosphorus-containing Y-type molecular sieve further comprises: collecting the solid product, then washing with water and drying to obtain a phosphorus-containing molecular sieve; the drying conditions are as follows: the temperature is 50-350 ℃; the time is 1-24 h.

13. The catalyst according to claim 12, wherein the drying temperature is 70 to 200 ℃.

14. The catalyst of claim 12, wherein the drying time is 2 to 6 hours.

15. The catalyst according to claim 1, wherein the weakly acidic silicon aluminum has an infrared B acidity value of 0.01 to 0.1mmol/g, a silicon content of 20 to 60 wt% in terms of silicon dioxide, and a pore volume of 0.5 to 1.0 mL/g; the weakly acidic silicon-aluminum is silicon-containing aluminum oxide and/or amorphous silicon-aluminum.

16. The catalyst of claim 1, wherein the first metal is molybdenum and/or tungsten; the second metal is at least one selected from iron, nickel and cobalt.

17. A process for preparing a hydrocracking catalyst according to any one of claims 1 to 16, characterized in that the process comprises: the impregnation liquid containing the metal precursor is contacted with the carrier for impregnation, and then the material obtained after the impregnation is dried.

18. The method of claim 17, wherein the method further comprises: mixing a phosphorus-containing Y-type molecular sieve, alumina, weakly acidic silicon aluminum, a peptizing agent and an optional lubricant, and then molding, drying and roasting to obtain the carrier.

19. The method of claim 17, wherein the metal precursor comprises a first metal precursor and a second metal precursor, wherein the first metal precursor is at least one selected from the group consisting of an inorganic acid of a first metal, an inorganic salt of a first metal, and a first metal organic compound; the inorganic salt is at least one selected from nitrate, carbonate, basic carbonate, hypophosphite, phosphate, sulfate and chloride; the organic substituent in the first metal organic compound is at least one selected from hydroxyl, carboxyl, amino, ketone, ether and alkyl;

20. The method of claim 17, wherein the impregnating solution further comprises an organic additive; the concentration of the organic additive is 2-300 g/L; the organic additive is at least one selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid, 1, 2-cyclohexanediamine tetraacetic acid, citric acid, tartaric acid, malic acid, ethylenediamine, diethylenetriamine, cyclohexanediamine tetraacetic acid, glycine, nitrilotriacetic acid, ethylenediaminetetraacetic acid, and ammonium ethylenediaminetetraacetate.

21. The method of claim 17, wherein the drying conditions are: the temperature is 80-350 ℃, and the time is 0.5-24 hours.

22. The method as claimed in claim 17, further comprising the step of drying the contacted material and then roasting the dried material under the following conditions: the temperature is 350-600 ℃, and the time is 0.2-12 hours.

23. Use of a hydrocracking catalyst as claimed in any one of claims 1 to 16 in the hydrocracking reaction of a hydrocarbon feedstock.

24. The use according to claim 23, wherein the hydrocarbon feedstock is at least one selected from the group consisting of straight run gas oil, vacuum gas oil, demetallized oil, atmospheric residue, deasphalted vacuum residue, coker distillate, catalytically cracked distillate, shale oil, tar sand oil, and coal liquefied oil;

the conditions of the hydrocracking reaction are as follows: the reaction temperature is 200-650 ℃; the reaction pressure is 3-24 MPa; the liquid hourly space velocity is 0.1-10 hours^-1(ii) a The volume ratio of hydrogen to oil is 100-5000.

25. The use according to claim 23, wherein the reaction temperature of the hydrocracking reaction is 300-510 ℃.

26. Use according to claim 23, wherein the hydrocracking reaction is carried out at a reaction pressure of 4-15 mpa.

27. The use of claim 23, wherein the liquid hourly space velocity of the hydrocracking reaction is in the range of 0.2 to 5 hours^-1。

28. The use according to claim 23, wherein the hydrocracking reaction has a hydrogen to oil volume ratio of 200-1000.