CN111632620B - Medium oil type hydrocracking catalyst - Google Patents

Medium oil type hydrocracking catalyst Download PDF

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Publication number
CN111632620B
CN111632620B CN202010550141.6A CN202010550141A CN111632620B CN 111632620 B CN111632620 B CN 111632620B CN 202010550141 A CN202010550141 A CN 202010550141A CN 111632620 B CN111632620 B CN 111632620B
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molecular sieve
oil type
medium oil
roasting
hydrocracking catalyst
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CN111632620A (en
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范文青
徐琳
张黎
刘长坤
肖文灿
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Sinochem Quanzhou Petrochemical Co Ltd
Sinochem Quanzhou Energy Technology Co Ltd
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Sinochem Quanzhou Petrochemical Co Ltd
Sinochem Quanzhou Energy Technology Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/166—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/66—Pore distribution
    • B01J35/695—Pore distribution polymodal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/10—Heat treatment in the presence of water, e.g. steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Abstract

The invention discloses a medium oil type hydrocracking catalyst and a preparation method thereof, wherein the medium oil type hydrocracking catalyst is prepared by adopting a modified Y molecular sieve subjected to simple hydrothermal treatment, so that the problems of low selectivity of middle distillate and low liquid product yield of the conventional catalyst are solved, and the yield benefit of the medium oil type hydrocracking process is remarkably improved.

Description

Medium oil type hydrocracking catalyst
Technical Field
The invention belongs to the technical field of catalyst preparation, and particularly relates to a medium oil type hydrocracking catalyst.
Background
The hydrocracking process is an oil refining process for converting a high boiling point raw material into middle distillates such as naphtha, kerosene, diesel oil and the like with low boiling points. Compared with catalytic cracking, the method has the advantages of high raw material adaptability, high yield of middle distillate and good quality. With the decline of the high sulfur fuel oil market and the increasing social demand for clean transportation fuel oil, the hydrocracking process becomes the core process of modern refineries.
Hydrocracking catalysts are typically bifunctional catalysts, generally comprising a bifunctional center: the catalyst is a metal center and is generally composed of a VIB metal or a VIB and VIII binary metal system, has hydrogenation/dehydrogenation functions, and can saturate aromatic hydrocarbon; the second is an acidic center with a cracking function, provided by amorphous silica alumina or molecular sieves (most commonly Y molecular sieves), for cracking long chain macromolecules.
When the hydrocracking catalyst prepared by the conventional Y molecular sieve is used in the hydrocracking process, middle distillate oil molecules, particularly kerosene fraction, easily undergo deep cracking reaction in microporous channels of the molecular sieve to generate C1-C4 gaseous light hydrocarbons with lower value, so that the selectivity of the middle distillate oil in the product is low, and the yield of the liquid product is low. Thus, there is a need to develop new hydrocracking catalysts with higher selectivity to middle distillates, particularly diesel distillates.
The pore structure of the hydrocracking catalyst is modified to form more mesoporous pores, so that the primary cracking products can be quickly diffused out of the microporous pores, the probability of deep cracking reaction is reduced, the generation of low-value C1-C4 gaseous hydrocarbon is reduced, and the selectivity of middle distillate oil and the yield of liquid products are improved. Since the cracking reaction usually occurs in the microporous channels of the molecular sieve, the formation of mesopores on the Y molecular sieve is the best way to modify the catalyst channel structure. Chemical methods such as strong acid, strong alkali or complexing agents are generally used for removing silicon or aluminum on a part of the framework of the Y molecular sieve, and then mesoporous on the molecular sieve is formed after high-temperature heat treatment. The ultra-stable Y molecular sieve used for the hydrocracking catalyst at present is generally subjected to dealumination treatment to adjust the strength and concentration of acid centers, and further strengthening treatment easily causes further reduction of the number of the acid centers to influence the activity of the catalyst; meanwhile, further desilication or aluminum of the molecular sieve framework is easy to cause the reduction of crystallinity, and the thermal stability of the molecular sieve is reduced, so that the catalyst is quickly deactivated in the operation process.
Disclosure of Invention
Aiming at the problems of low selectivity to middle distillate and low liquid product yield of the existing middle oil type hydrocracking catalyst, the invention provides a novel middle oil type hydrocracking catalyst and a preparation method thereof.
In order to achieve the above purpose, the invention adopts the following technical scheme:
one of the purposes of the invention is to provide a medium oil type hydrocracking catalyst, which comprises the following components:
(a) A metal of group VIII element or an oxide thereof;
(b) A metal of group VIB element or an oxide thereof;
(c) Amorphous silicon aluminum;
(d) Alumina;
(e) And (3) modifying the Y molecular sieve.
In the technical scheme, the component (a) is 0.1-35 parts by weight, preferably 15-25 parts by weight.
In the technical scheme, the component (b) is 0.1-10 parts by weight, preferably 4-8 parts by weight.
In the technical scheme, the component (c) is 1-60 parts by weight, preferably 20-40 parts by weight.
In the technical scheme, the component (d) is 1-80 parts by weight, preferably 20-50 parts by weight.
In the technical scheme, the component (e) is 0.1-30 parts by weight, preferably 1-10 parts by weight.
In the above technical solution, the group VIII element is at least one selected from Co and Ni.
In the above technical scheme, the group VIB element is at least one selected from Mo or W.
In the technical scheme, the amorphous silicon aluminum is obtained by roasting 4h at 500 ℃ in advance in an air atmosphere; its specific surfaceThe product is 200-600 m 2 Per gram, the pore volume is 0.5-1.5 cm 3 Preferably 1.1 to 1.5 cm/g 3 /g; siO in weight percent 2 The content is 20-80%.
In the technical scheme, the alumina is obtained by roasting pseudo-boehmite at 500 ℃ for 4h in an air atmosphere; the specific surface area is 150-400 m 2 Per gram, the pore volume is 0.3-0.8 cm 3 And/g, wherein the content of Na element is less than or equal to 0.2 percent in percentage by weight.
In the technical scheme, the modified Y molecular sieve is prepared by adding the Y molecular sieve and the ionic surfactant into ammonia water, fully stirring at room temperature, placing the mixture into a high-pressure reaction kettle for hydrothermal treatment, and then filtering and drying.
Wherein the Y molecular sieve is a hydrogen type molecular sieve, and the specific surface area of the Y molecular sieve is 400-900 m 2 Preferably 500 to 800 m 2 /g; the total pore volume is 0.30-0.80 cm 3 /g, wherein the mesopore volume is less than 0.15 and 0.15 cm 3 The molar ratio of Si/Al is 5-30, and the unit cell size is 24.25-24.45。
The mass ratio of the Y molecular sieve to the ionic surfactant is 1: (0.1-3); the ionic surfactant is specifically a cationic surfactant, preferably an ammonium salt or an amine salt cationic surfactant, and more preferably at least one of cetyltrimethylammonium chloride (CTAC) and cetyltrimethylammonium bromide (CTAB).
The mass ratio of the used Y molecular sieve to the ammonia water is 1: (1-500); in weight percent, the ammonia monohydrate (NH) 4 OH) content is 0.5-5%.
The temperature of the hydrothermal treatment is 100-200 ℃ and the time is 1-48 hours; the drying temperature is 80-200 ℃ and the drying time is 1-24 h.
Another object of the present invention is to provide a method for preparing the medium oil type hydrocracking catalyst, which comprises the steps of:
(1) Uniformly mixing pseudo-boehmite, amorphous silicon aluminum and a modified Y molecular sieve, adding an acid solution, fully kneading, forming, drying, heating to a roasting target temperature in a nitrogen atmosphere, and then switching to an air atmosphere for roasting to obtain a catalyst carrier;
(2) Dispersing a compound containing VIB element and a compound containing VIII element in a solvent for impregnating the catalyst carrier obtained in the step (1), and then drying and roasting to obtain the medium oil type hydrocracking catalyst.
In the above technical solution, the acid solution in step (1) may be inorganic acid such as sulfuric acid, hydrochloric acid, and nitric acid, or organic acid such as formic acid, acetic acid, and citric acid; the concentration of the acid solution is 0.5wt% to 5wt%, preferably 1wt% to 3wt%.
In the above technical scheme, the size and shape of the molded product in the step (1) are preferably similar to those of the conventional hydrocracking commercial catalyst, and more preferably the extrudate with a diameter of 1.5-3.5 nm and a length of 3-12 nm is prepared as a round or clover cross section.
In the technical scheme, the drying temperature in the step (1) is 80-200 ℃ and the drying time is 2-24 hours; the temperature rising rate under the nitrogen atmosphere is 1-20 ℃/min, the target temperature is 400-650 ℃, and the roasting time under the air atmosphere is 3-12 h.
In the above technical scheme, the compound containing the group VIB element and the compound containing the group VIII element in the step (2) are not particularly limited, and may be reasonably selected by those skilled in the art.
In the above-mentioned technical scheme, the solvent used in the step (2) is not particularly limited as long as the impregnation supporting operation can be realized, and the solvents may be directly dissolved, or dissolved by adjusting the pH, or those solvents capable of forming a colloid or forming a colloid by adjusting the pH, or may be single solvents or mixed solvents.
In the technical scheme, the drying temperature in the step (2) is 80-200 ℃ and the drying time is 2-24 hours; the roasting temperature is 400-600 ℃ and the roasting time is 2-12 h.
The modification of the Y molecular sieve under the milder hydrothermal condition can be directly used for preparing the catalyst only by simple filtration and separation without high-temperature heat treatment. Therefore, under the condition of not damaging the framework structure of the molecular sieve, the improvement of the pore structure of the molecular sieve is realized, more mesoporous pores are formed in the prepared hydrocracking catalyst, the primary cracking products can be quickly diffused out of the microporous pores, the probability of deep cracking reaction is reduced, the generation of low-value C1-C4 gaseous hydrocarbon is reduced, and the selectivity of middle distillate and the yield of liquid products are improved.
Compared with the existing hydrocracking catalyst, the middle oil type hydrocracking catalyst prepared by using the modified Y molecular sieve can improve the selectivity of middle distillate oil on the basis of improving the activity of the catalyst, and the yield of liquid products is also improved. The production benefit can be obviously improved for the oil type hydrocracking device in production.
Detailed Description
In order to make the contents of the present invention more easily understood, the technical scheme of the present invention will be further described with reference to the specific embodiments, but the present invention is not limited thereto.
The amorphous silicon aluminum is baked in advance at 500 ℃ under the air atmosphere for 4 h; the specific surface area is 200-600 m 2 Per gram, the pore volume is 0.5-1.5 cm 3 /g; siO in weight percent 2 The content is 20-80%.
Example 1
15.0 g of Y molecular sieve powder, 10.0g of CTAC was added to 1000 g of ammonia (NH) 4 OH content of 1 wt%) at room temperature, stirring thoroughly for 30 min, then placing in a high-pressure reaction kettle, performing hydrothermal treatment at 170 ℃ for 24h, filtering and drying at 120 ℃ for 12h to obtain modified Y molecular sieve powder Y-1.
Example 2
15.0 g of Y molecular sieve powder, 20.0g of CTAC was added to 350 g of ammonia (NH) 4 OH content was 2 wt%) and stirred well at room temperature for 60 minutes, then placed in a high pressure autoclave, hydrothermally treated at 180℃for 20 h, then filtered and dried at 140℃for 30 hours to obtain modified Y molecular sieve powder Y-2.
Comparative example 1
Will be 15.0g Y molecular sieve powder, 20.0g CTAC were added to 350 g ammonia (NH) 4 OH content was 2 wt%) and stirred well at room temperature for 60 minutes, then filtered and dried at 140℃for 30 hours to give modified Y molecular sieve powder Y-3.
Table 1 shows the comparison results of the pore volumes of the Y molecular sieves and the prepared modified Y molecular sieves Y-1, Y-2 and Y-3 (before pore volume measurement, Y-1, Y-2 and Y-3 were each baked in an air atmosphere for 6 hours after heating to 560 ℃ in a nitrogen atmosphere).
Table 1, Y molecular sieves pore volume comparison results
As can be seen from Table 1, compared with the Y molecular sieve, the mesoporous volume of the modified Y-1 and Y-2 molecular sieves is increased, especially the increase of 2-10 nm pores is most obvious, and the pore volume of the Y-3 molecular sieve modified by the surfactant is slightly increased.
Example 3
10.0g of modified Y molecular sieve powder Y-1 prepared in example 1, 10.0g amorphous silica-alumina powder and 12.0 g pseudo-boehmite powder were uniformly mixed, then 1.5wt% of nitric acid solution was added, and after sufficient kneading, clover-shaped particles having a length of 3 to 10 mm and a diameter of 2 mm were extruded, dried at 140℃for 10 hours, and then heated to 560℃under nitrogen atmosphere, and then switched to air atmosphere for calcination for 6 hours, to obtain catalyst carrier S-1.
Example 4
Nickel nitrate (Ni (NO) that provides sufficient nickel oxide (NiO) in the final catalyst 3 ) 2 ·6H 2 O) and enough tungsten trioxide (WO 3 ) Ammonium meta-tungstate ((NH) 4 ) 10 W 12 O 41 ·xH 2 O) was dispersed in deionized water, and then used to impregnate the catalyst support S-1 obtained in example 3, and dried at 120℃for 10 hours, and finally calcined at 550℃for 6 hours, to obtain catalyst C-1.
Example 5
10.0g of modified Y molecular sieve powder Y-2 prepared in example 2, 10.0g amorphous silicon aluminum powder and 12.0 g pseudo-boehmite powder are uniformly mixed, then 1.5wt% of nitric acid solution is added, fully kneaded and extruded into clover-shaped particles with the length of 3-10 mm and the diameter of 2 mm, dried for 10 hours at 140 ℃, then heated to 560 ℃ in nitrogen atmosphere, and then switched to air atmosphere for roasting for 6 hours, thus obtaining the catalyst carrier S-2.
Example 6
Nickel nitrate (Ni (NO) that provides sufficient nickel oxide (NiO) in the final catalyst 3 ) 2 ·6H 2 O) and enough tungsten trioxide (WO 3 ) Ammonium meta-tungstate ((NH) 4 ) 10 W 12 O 41 ·xH 2 O) was dispersed in deionized water and then used to impregnate the catalyst support S-2 obtained in example 5, and then dried at 120℃for 10 hours and finally calcined at 550℃for 6 hours to obtain catalyst C-2.
Comparative example 2
(1) Uniformly mixing 10.0g of the Y-3 powder prepared in comparative example 1, 10.0. 10.0g amorphous silicon aluminum powder and 12.0 g pseudo-boehmite powder, adding 1.5wt% of nitric acid solution, fully kneading, extruding into clover-shaped particles with the length of 3-10 mm and the diameter of 2 mm, drying at 140 ℃ for 10 hours, heating to 560 ℃ under nitrogen atmosphere, and then switching to air atmosphere for roasting for 6 hours to obtain the catalyst carrier S-3.
(2) Nickel nitrate (Ni (NO) that provides sufficient nickel oxide (NiO) in the final catalyst 3 ) 2 ·6H 2 O) and enough tungsten trioxide (WO 3 ) Ammonium meta-tungstate ((NH) 4 ) 10 W 12 O 41 ·xH 2 O) is dispersed in deionized water, then used for impregnating the catalyst carrier S-3, dried for 10 hours at 120 ℃, and finally baked for 6 hours at 550 ℃ to obtain the catalyst C-3.
Comparative example 3
(1) Uniformly mixing 10.0g Y molecular sieve powder, 10.0g amorphous silicon aluminum powder and 12.0 g pseudo-boehmite powder, adding 1.5wt% nitric acid solution, fully kneading, extruding into clover-shaped particles with the length of 3-10 mm and the diameter of 2 mm, drying at 140 ℃ for 10 hours, heating to 560 ℃ under nitrogen atmosphere, and then switching to air atmosphere for roasting for 6 hours to obtain the catalyst carrier S-4.
(2) Nickel nitrate (Ni (NO) that provides sufficient nickel oxide (NiO) in the final catalyst 3 ) 2 ·6H 2 O) and enough tungsten trioxide (WO 3 ) Ammonium meta-tungstate ((NH) 4 ) 10 W 12 O 41 ·xH 2 O) is dispersed in deionized water, then is used for impregnating the carrier S-3 obtained in the step (1), is dried for 10 hours at 120 ℃, and is finally roasted for 6 hours at 550 ℃ to obtain the catalyst C-4.
Comparative example 4
(1) Uniformly mixing 10.0g Y molecular sieve powder, 10.0g amorphous silicon aluminum powder and 12.0 g pseudo-boehmite powder, adding 1.5wt% nitric acid solution, fully kneading, extruding into clover-shaped particles with the length of 3-10 mm and the diameter of 2 mm, drying at 140 ℃ for 10 hours, heating to 560 ℃ in air atmosphere, and roasting for 6 hours to obtain the catalyst carrier S-5.
(2) Nickel nitrate (Ni (NO) that provides sufficient nickel oxide (NiO) in the final catalyst 3 ) 2 ·6H 2 O) and enough tungsten trioxide (WO 3 ) Ammonium meta-tungstate ((NH) 4 ) 10 W 12 O 41 ·xH 2 O) is dispersed in deionized water, then is used for impregnating the carrier S-4 obtained in the step (1), is dried for 10 hours at 120 ℃, and is finally roasted for 6 hours at 550 ℃ to obtain the catalyst C-5.
The pore volume results of the catalyst supports obtained in examples 3, 5 and comparative examples 2-4 are shown in Table 2.
TABLE 2 catalyst support pore volume
As can be seen from Table 2, the mesoporous volume of the carriers S-1 and S-2 was increased, particularly the increase in pores of 2 to 10nm was most remarkable, as compared with the carriers S-3, S-4 and S-5 prepared in the comparative examples.
Example 7
The catalyst performance was evaluated using a once-through 50 mL small hydrogenation evaluation unit. H was used at a volume fraction of 5% before evaluation 2 S and 95% H 2 The catalyst is presulfided by the composed mixed gas. The raw material used for evaluating the performance of the catalyst is hydrocracking circulating oil, and the properties and the reaction process conditions are shown in tables 3 and 4. The reaction temperature was adjusted as required to ensure that the conversion in mass percent was maintained at 68% for 100 hours. The comparative results of the reactivity of each catalyst are shown in Table 5.
TABLE 3 Properties of raw oil
TABLE 4 reaction process conditions
Table 5 catalyst evaluation results
As can be seen from Table 5, the activities of catalysts C-1 and C-2 are slightly better than those of the comparative examples at the same conversion, and the difference is not great, but the selectivity of middle distillate oil, particularly the selectivity of diesel oil distillate oil is obviously improved (3-4 percent improvement), the generation of C1-C4 is reduced, and the liquid yield is also improved.
The foregoing description is only of the preferred embodiments of the invention, and all changes and modifications that come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.

Claims (7)

1. A medium oil type hydrocracking catalyst, which is characterized in that: the composition comprises the following components:
(a) A metal of group VIII element or an oxide thereof;
(b) A metal of group VIB element or an oxide thereof;
(c) Amorphous silicon aluminum;
(d) Alumina;
(e) Modifying a Y molecular sieve;
15-25 parts of component (a), 4-8 parts of component (b), 20-40 parts of component (c), 20-50 parts of component (d) and 1-10 parts of component (e) by weight;
the VIII group element is selected from at least one of Co or Ni;
the VIB element is at least one selected from Mo or W;
the amorphous silicon aluminum is obtained by roasting 4h at 500 ℃ in advance under the air atmosphere;
the modified Y molecular sieve is prepared by adding a Y molecular sieve and an ionic surfactant into ammonia water, fully stirring at room temperature, placing the mixture into a high-pressure reaction kettle for hydrothermal treatment, and then filtering and drying the mixture; wherein the mass ratio of the Y molecular sieve to the ionic surfactant to the ammonia water is 1 (0.1-3) (1-500), the temperature of the hydrothermal treatment is 100-200 ℃ and the time is 1-48 h.
2. The medium oil type hydrocracking catalyst as claimed in claim 1, wherein: the specific surface area of the amorphous silicon aluminum is 200-600 m 2 Per gram, the pore volume is 0.5-1.5 cm 3 Per gram, in weight percent, siO 2 The content is 20-80%.
3. The medium oil type hydrocracking catalyst as claimed in claim 1, wherein: the alumina is obtained by roasting pseudo-boehmite at 500 ℃ for 4h in an air atmosphere; the specific surface area is 150-400 m 2 Per gram, the pore volume is 0.3-0.8 cm 3 And/g, wherein the content of Na element is less than or equal to 0.2 percent in percentage by weight.
4. The medium oil type hydrocracking catalyst as claimed in claim 1, characterized in thatThe method comprises the following steps: the Y molecular sieve used for preparing the modified Y molecular sieve is a hydrogen type molecular sieve, and the specific surface area of the Y molecular sieve is 400-900 m 2 Per gram, the total pore volume is 0.30-0.80 cm 3 /g, wherein the mesopore volume is less than 0.15 and 0.15 cm 3 The molar ratio of Si/Al is 5-30, and the unit cell size is 24.25-24.45；
The ionic surfactant is specifically a cationic surfactant;
the content of the ammonia monohydrate in the ammonia water is 0.5-5% by weight percent;
the drying temperature is 80-200 ℃ and the drying time is 1-24 h.
5. The medium oil type hydrocracking catalyst as claimed in claim 1, wherein: the preparation method comprises the following steps:
(1) Uniformly mixing pseudo-boehmite, amorphous silicon aluminum and a modified Y molecular sieve, adding an acid solution, fully kneading, forming, drying, heating to a roasting target temperature in a nitrogen atmosphere, and then switching to an air atmosphere for roasting to obtain a catalyst carrier;
(2) Dispersing a compound containing VIB element and a compound containing VIII element in a solvent for impregnating the catalyst carrier obtained in the step (1), and then drying and roasting to obtain the medium oil type hydrocracking catalyst.
6. The medium oil type hydrocracking catalyst as claimed in claim 5, wherein: the drying temperature in the step (1) is 80-200 ℃ and the drying time is 2-24 hours; the temperature rising rate under the nitrogen atmosphere is 1-20 ℃/min, the target temperature is 400-650 ℃, and the roasting time under the air atmosphere is 3-12 h.
7. The medium oil type hydrocracking catalyst as claimed in claim 5, wherein: the drying temperature in the step (2) is 80-200 ℃ and the drying time is 2-24 hours; the roasting temperature is 400-600 ℃ and the roasting time is 2-12 h.
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