CN111117696B

CN111117696B - Hydrocracking method

Info

Publication number: CN111117696B
Application number: CN201811277964.5A
Authority: CN
Inventors: 莫昌艺; 赵阳; 吴昊; 胡志海; 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: 2018-10-30
Filing date: 2018-10-30
Publication date: 2021-11-02
Anticipated expiration: 2038-10-30
Also published as: CN111117696A

Abstract

A hydrocracking method, raw oil and hydrogen are mixed and then sequentially pass through a hydrofining reaction zone and a hydrocracking reaction zone, reaction products are separated to obtain heavy naphtha and jet fuel components, and the hydrocracking reaction zone is filled with three different hydrocracking catalysts from top to bottom; the volume of the total catalyst in the hydrocracking reaction zone is calculated by 100 percent, the volume fraction of the hydrocracking catalyst I is 15 to 35 percent, the volume fraction of the hydrocracking catalyst II is 35 to 65 percent, and the volume fraction of the hydrocracking catalyst III is 20 to 40 percent. The method provided by the invention can give consideration to both the activity and the stability of the hydrocracking catalyst, and can produce heavy naphtha and jet fuel components to the maximum extent under high conversion rate.

Description

Hydrocracking method

Technical Field

The invention belongs to a processing method of distillate oil or secondary processing oil under a high-pressure hydrogen condition, and particularly relates to a hydrocracking method for producing heavy naphtha and jet fuel by using the distillate oil or the secondary processing oil.

Background

In recent years, the continuous development of the economy of China brings about the continuous increase of the requirements of aviation transportation fuels and aromatic hydrocarbon raw materials. The hydrocracking process can convert heavy distillate oil into light products, heavy naphtha in the light products can be used as a catalytic reforming raw material to produce aromatic hydrocarbon, and jet fuel fraction can be used as high-quality No. 3 jet fuel. However, the problems of partial diesel oil production, insufficient heavy naphtha yield and the like exist in the domestic single-stage one-time pass hydrocracking device for producing middle distillate oil (diesel oil and jet fuel) and producing high-quality tail oil and heavy fuel oil at the same time, so that the development of the hydrocracking technology for producing the heavy fuel oil and the jet fuel to the maximum extent and meeting the market demand and simultaneously producing little or no diesel oil has important practical significance.

CN104611019A discloses a low-energy hydrocracking method for producing high-quality jet fuel. The method mainly produces heavy naphtha and aviation kerosene by a catalyst grading method, and is characterized in that raw oil and hydrogen are mixed and then sequentially pass through a hydrofining reaction zone and a hydrocracking reaction zone, the conversion rate of the cracking reaction is controlled to be about 70%, reaction effluent is obtained, and products are obtained by separating the reaction effluent.

CN104611025B discloses a low-energy-consumption hydrocracking method for producing high-quality chemical raw materials. The method is characterized in that at least two hydrocracking catalysts are filled in the hydrocracking reaction zone, a catalyst I is filled upstream to modify a Y molecular sieve by 30-70%, a catalyst II contains 15-50% of the Y molecular sieve, and the Y molecular sieve in the catalyst I is 10-30% higher than the catalyst II. The filling volume ratio of the hydrocracking catalyst I to the hydrocracking catalyst II is 1: 5-5: 1.

In the prior art, the heavy naphtha and jet fuel are produced by a single-stage once-through hydrocracking technology, and the problems are that firstly, the conversion rate is lower under the condition of the existing single-stage once-through hydrocracking technology, and the yield of the heavy naphtha and jet fuel in the product is insufficient. Secondly, the existing hydrocracking catalyst with higher cracking activity is adopted, so that the selectivity of the product heavy naphtha and jet fuel is poor, and the hydrocracking catalyst is high in cracking activity and sensitive to temperature, so that the hydrocracking catalyst is easy to fluctuate in the operation process of the device, and great influence is brought to the operation stability of the device. In addition, when a hydrocracking catalyst having relatively low cracking activity is used, in order to increase the yield of heavy naphtha and jet fuel, it is necessary to increase the hydrocracking reaction temperature, which causes instability in the activity of the hydrocracking catalyst, thereby shortening the plant operation cycle.

Disclosure of Invention

The invention provides a hydrocracking method, aiming at solving the technical problems of low component yield, low selectivity and short device operation period of heavy naphtha and jet fuel in the prior art.

The hydrocracking method provided by the invention comprises the following steps: raw oil and hydrogen are mixed and then sequentially pass through a hydrofining reaction zone and a hydrocracking reaction zone, reaction products are obtained and separated to obtain heavy naphtha, jet fuel components and tail oil,

the conversion rate of the raw materials is controlled to be 79-92 percent;

the hydrofining reaction area is filled with a hydrofining catalyst; the hydrocracking reaction zone is sequentially filled with a hydrocracking catalyst I, a hydrocracking catalyst II and a hydrocracking catalyst III from top to bottom;

the hydrocracking catalyst I comprises a carrier and an active metal oxide loaded on the carrier, wherein the content of the active metal oxide is 22-32 percent and the balance is the carrier on the basis of the whole weight of the hydrocracking catalyst I, the carrier consists of a heat-resistant inorganic oxide and a Y-type molecular sieve, and the weight fraction of the Y-type molecular sieve in the carrier is 40-65 percent;

the hydrocracking catalyst II comprises a carrier and an active metal oxide loaded on the carrier, wherein the content of the active metal oxide is 26-35 percent and the balance is the carrier by taking the whole weight of the hydrocracking catalyst II as the reference, the carrier consists of a heat-resistant inorganic oxide and a Y-type molecular sieve, and the weight fraction of the Y-type molecular sieve in the carrier is 40-65 percent;

the hydrocracking catalyst III comprises a carrier and an active metal oxide loaded on the carrier, wherein the content of the active metal oxide is 26-35 percent and the balance is the carrier by taking the whole weight of the hydrocracking catalyst III as a reference, the carrier consists of a heat-resistant inorganic oxide and a Y-type molecular sieve, and the weight fraction of the Y-type molecular sieve in the carrier is 15-25 percent;

the volume of the total catalyst in the hydrocracking reaction zone is 100 percent, the volume fraction of the hydrocracking catalyst I is 15 to 35 percent, the volume fraction of the hydrocracking catalyst II is 35 to 65 percent, and the volume fraction of the hydrocracking catalyst III is 20 to 40 percent.

In order to better balance the relationship between the activity and stability of the hydrocracking catalyst and the product selectivity, in the preferred case of the invention, the content of the active metal oxide in the hydrocracking catalyst II is the same as that in the hydrocracking catalyst III and is 4-8% higher than that in the hydrocracking catalyst I.

Under the preferable condition of the invention, the content of the Y-type molecular sieve in the carrier of the hydrocracking catalyst I is the same as that of the Y-type molecular sieve in the carrier of the hydrocracking catalyst II, and is 1.8-2.5 times of that of the Y-type molecular sieve in the carrier of the hydrocracking catalyst III.

The distillation range of the raw oil is 200-580 ℃, the mass fraction of sulfur is 0.2-2.5%, and the mass fraction of nitrogen is 700-3000 mug/g.

In one preferred embodiment of the present invention, the raw oil is selected from vacuum wax oils with paraffin mass fraction of 1% to 28%, and more preferably cycloalkyl or intermediate vacuum wax oils with paraffin mass fraction of 1% to 20%.

In a preferred embodiment of the present invention, the raw oil is a mixed raw material of vacuum wax oil and one or more selected from deasphalted oil, coal tar, direct and indirect coal liquefaction oil and catalytic cracking light cycle oil, wherein the mass fraction of the vacuum wax oil is 75% to 99%, and the mass fraction of paraffin of the mixed raw material is 1% to 28%, preferably 1% to 20%.

Under the preferable condition, the reaction product is subjected to gas-liquid separation through a high-pressure separator, the obtained liquid phase material flow enters a low-pressure separator for further gas-liquid separation, and then the obtained liquid phase material flow enters a fractionation system for fractionation to obtain gas, light naphtha, heavy naphtha, jet fuel components and tail oil, wherein the distillation range of the heavy naphtha is 65-150 ℃, the distillation range of the jet fuel components is 150-282 ℃, and the distillation range of the tail oil is more than 282 ℃. Wherein the yield of the sum of the heavy naphtha and jet fuel components can reach 80 percent at most. Controlling the conversion rate of raw materials to be 79-92%, preferably 82-88%, wherein the conversion rate of raw materials is defined as: the conversion rate of raw materials is 100 percent and the yield of tail oil.

In a preferred case, the hydrofinishing reaction conditions are: the hydrogen partial pressure is 6.0MPa to 20.0MPa, the reaction temperature is 280 ℃ to 400 ℃, and the liquid hourly space velocity is 0.5h^-1～6h^-1The volume ratio of hydrogen to oil is 300-2000.

In a preferred case, the hydrocracking reaction conditions are: the hydrogen partial pressure is 6.0MPa to 20.0MPa, the reaction temperature is 290 ℃ to 420 ℃, and the liquid hourly space velocity is 0.3h^-1～5h^-1The volume ratio of hydrogen to oil is 300-2000.

The hydrorefining catalyst of the present invention is not particularly limited, and any catalyst satisfying the hydrorefining function may be used, for example, a commercially available hydrorefining catalyst or a laboratory hydrorefining catalyst. Preferably, the hydrofinishing catalyst is at least one catalyst selected from a group VIB non-noble metal, or at least one selected from a group VIII non-noble metal, or a combination thereof, supported on alumina or/and silica-alumina. Further preferably, the group VIII non-noble metal is selected from nickel and/or cobalt, the group VIB non-noble metal is selected from molybdenum and/or tungsten, based on the total weight of the hydrorefining catalyst, the total content of nickel and/or cobalt calculated by oxides is 1 wt% to 15 wt%, the total content of molybdenum and/or tungsten calculated by oxides is 5 wt% to 40 wt%, and the balance is a carrier.

The invention is that three hydrocracking catalysts are filled in a hydrocracking reaction zone in a grading way, under the preferable condition, the hydrocracking catalyst I comprises a carrier and an active metal component loaded on the carrier, and the carrier consists of a heat-resistant inorganic oxide and a Y-shaped molecular sieve; the heat-resistant inorganic oxide is selected from one or more of silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from VIB group metals and VIII group metals; based on the hydrocracking catalyst I as a whole, calculated by oxides, 14-30 wt% of VIB group metal, 2-8 wt% of VIII group metal and the balance of carrier; based on the carrier, the Y-type molecular sieve accounts for 40-65 wt%, and the rest is heat-resistant inorganic oxide. More preferably, the amount of the Y-type molecular sieve is 40 to 65 wt%, the amount of the alumina is 20 to 40 wt%, and the amount of the amorphous aluminum silicate is 0 to 32 wt%, based on the carrier.

In a preferred case, the hydrocracking catalyst II comprises a carrier and an active metal component loaded on the carrier, wherein the carrier consists of a heat-resistant inorganic oxide and a Y-type molecular sieve; the heat-resistant inorganic oxide is selected from one or more of silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from VIB group metals and VIII group metals; taking the hydrocracking catalyst II as a whole as a reference, and taking the oxide as the basis, wherein the weight percentage of the VIB group metal is 15-33%, the weight percentage of the VIII group metal is 2-8%, and the balance is a carrier; based on the carrier, 40-65 wt% of Y-type molecular sieve and the balance of heat-resistant inorganic oxide.

In a preferred case, the hydrocracking catalyst III comprises a carrier and an active metal component loaded on the carrier, wherein the carrier consists of a heat-resistant inorganic oxide and a Y-type molecular sieve; the heat-resistant inorganic oxide is selected from one or more of silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from VIB group metals and VIII group metals; taking the hydrocracking catalyst III as a whole as a reference, and taking the oxide as the basis, 15-33 wt% of VIB group metal, 2-8 wt% of VIII group metal and the balance of carrier; based on the carrier, the weight of the Y-type molecular sieve is 15-25 percent, and the balance is heat-resistant inorganic oxide.

The treatment method provided by the invention can give consideration to both the activity and the stability of the hydrocracking catalyst, and can produce heavy naphtha and jet fuel components to the maximum extent under high conversion rate.

Detailed Description

The following examples further illustrate the hydrocracking process provided by the present invention, but the invention is not to be so limited.

In the examples of the present invention and the comparative examples,

the yield of heavy naphtha is defined as: the weight percentage of the heavy naphtha fraction (65-150 ℃) cut from the full fraction product by a fractionating tower to the raw material;

the yield of jet fuel components is defined as: the weight percentage of jet fuel components (150-282 ℃) cut out of the full fraction product by a fractionating tower to the raw material;

the yield of the tail oil fraction is defined as: the weight percentage of the tail oil fraction (>282 ℃) cut out of the full-range product by the fractionating tower to the raw material.

The hydrofining catalyst used in the examples was sold under the trade designation RN-410 and was produced by Changjingtie of petrochemical Co., Ltd.

The properties of the raw material A, B, C used in the examples and comparative examples are shown in table 1. Wherein, the raw material C is obtained by mixing 15 wt% of catalytic diesel oil with two raw materials A and B with different paraffin mass fractions and a wax oil raw material, and the paraffin mass fraction of the raw material C is 15.4%.

In comparative example 1, example 1 and example 2

The hydrocracking catalyst I comprises, in terms of oxide, 23.5 wt% of W, 3.0 wt% of Ni and the balance of a carrier; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst II comprises 28.0 wt% of W, 4.0 wt% of Ni and the balance of a carrier, wherein the W is calculated by oxide; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst III comprises 28.0 wt% of W, 4.0 wt% of Ni and the balance of a carrier, wherein the W is calculated by oxides; based on the carrier, the content of the Y-type molecular sieve is 20 percent by weight, and the balance is alumina.

Comparative example 1

The raw material A and hydrogen are mixed and then pass through a hydrofining reaction zone and a hydrocracking reaction zone to be sequentially contacted with a hydrofining catalyst and three hydrocracking catalysts for reaction, the conversion rate of the raw material is controlled to be 85%, and the obtained reaction effluent is separated to obtain heavy naphtha and jet fuel components. Catalyst grading schemes, process condition parameters, product yields and property data are listed in table 2.

From the data in table 2, the yields of heavy naphtha and jet fuel components obtained for feed a were 33.76% and 39.50%, respectively.

Example 1

And the raw material B is mixed with hydrogen and then passes through a hydrofining reaction zone and a hydrocracking reaction zone to be sequentially contacted with a hydrofining catalyst and three hydrocracking catalysts for reaction, the conversion rate of the raw material is controlled to be 85%, and the obtained reaction effluent is separated to obtain heavy naphtha and jet fuel components. Catalyst grading schemes, process condition parameters, product yields and property data are listed in table 2.

As can be seen from the data in table 2, the yields of heavy naphtha and product jet fuel components from feed B are 36.15% and 41.63%, respectively.

Example 2

And the raw material C is mixed with hydrogen and then passes through a hydrofining reaction zone and a hydrocracking reaction zone to be sequentially contacted with a hydrofining catalyst and three hydrocracking catalysts for reaction, the conversion rate of the raw material is controlled to be 85%, and the obtained reaction effluent is separated to obtain heavy naphtha and jet fuel components. Catalyst grading schemes, process condition parameters, product yields and property data are listed in table 2.

As can be seen from the data in table 2, the yields of heavy naphtha and jet fuel components obtained for feed C are 39.21% and 41.34%, respectively.

It can be seen that the yield of the heavy naphtha and jet fuel components can be obviously increased by adopting the optimized raw oil of the method under the same conversion depth.

Comparative example 2 and example 3

In comparative example 2

The hydrocracking catalyst I comprises 27.0 wt% of W, 3.0 wt% of Ni and the balance of a carrier, wherein the W is calculated by oxides; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst II comprises 27.0 wt% of W, 3.0 wt% of Ni and the balance of a carrier, calculated by oxide; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst III comprises 27.0 wt% of W, 3.0 wt% of Ni and the balance of a carrier, calculated by oxide; based on the carrier, the content of the Y-type molecular sieve is 20 percent by weight, and the balance is alumina.

In comparative example 2

And the raw material B is mixed with hydrogen and then passes through a hydrofining reaction zone and a hydrocracking reaction zone to be sequentially contacted with a hydrofining catalyst and three hydrocracking catalysts for reaction, the conversion rate of the raw material is controlled to be 85%, and the obtained reaction effluent is separated to obtain heavy naphtha and jet fuel components. Catalyst grading schemes, process condition parameters, product yields and property data are listed in table 3.

As can be seen from the data in table 3, the yields of the heavy naphtha and product jet fuel components obtained in comparative example 2 are 36.83% and 39.75%, respectively, and the potential aromatics content of the heavy naphtha fraction is 48.0%.

In example 3

The hydrocracking catalyst I comprises 24.0 wt% of W, 3.0 wt% of Ni and the balance of a carrier, wherein the W is calculated by oxides; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst II comprises 27.0 wt% of W, 4.0 wt% of Ni and the balance of a carrier, calculated by oxide; based on the carrier, the content of the Y-type molecular sieve is 50 wt%, and the balance is alumina.

The hydrocracking catalyst III comprises 27.0 wt% of W, 4.0 wt% of Ni and the balance of a carrier, calculated by oxide; based on the carrier, the content of the Y-type molecular sieve is 20 percent by weight, and the balance is alumina.

As can be seen from the data in table 3, the yields of the heavy naphtha and product jet fuel components obtained in example 3 were 37.15% and 41.35%, respectively, and the potential aromatics content of the heavy naphtha fraction was 56.0%.

From the above, by adopting the catalyst grading scheme provided by the invention, not only the yield of the heavy naphtha and jet fuel components is high, but also the potential aromatic content of the heavy naphtha fraction is higher.

Comparative examples 3 to 4, examples 4 to 5

The same hydrocracking catalyst as in example 3 and the same hydrocracking catalyst packing volume ratio were used in comparative example 3, comparative example 4, example 4 and example 5.

And the raw material B is mixed with hydrogen and then passes through a hydrofining reaction zone and a hydrocracking reaction zone, and then passes through the hydrofining reaction zone and the hydrocracking reaction zone to sequentially contact with a hydrofining catalyst and three hydrocracking catalysts for reaction, and the obtained reaction effluent is separated to obtain heavy naphtha and jet fuel components. Catalyst grading schemes, process condition parameters and product yields and property data are listed in table 4.

Except that in comparative example 3 the feed conversion was controlled to 75% and the yields of heavy naphtha and jet fuel components were 26.76% and 41.04%, respectively.

In comparative example 4 the feed conversion was controlled to 93% and the heavy naphtha and jet fuel component yields were 43.73% and 27.60%, respectively.

In example 4 the feedstock conversion was controlled to 83% and the heavy naphtha and jet fuel component yields were 35.78% and 41.75%, respectively.

Feed conversion was controlled to 87% in example 5, and yields of heavy naphtha and jet fuel components were 38.35% and 40.85%, respectively.

It can be seen that either insufficient or excessive feedstock conversion results in insufficient overall yields of the product heavy naphtha and jet fuel components, and that the yield of the product heavy naphtha and jet fuel components can be significantly increased with the preferred conversion range of the present invention.

Comparative examples 5 to 6, examples 6 to 7

Comparative example 5, comparative example 6, example 6 and example 7 used the same hydrocracking catalyst as in example 3.

And mixing the raw oil B with hydrogen, sequentially passing through a hydrofining reaction zone and a hydrocracking reaction zone, controlling the conversion rate of the raw material to be 82%, and separating the obtained reaction effluent to obtain heavy naphtha and jet fuel components. The process condition parameters, catalyst grading scheme, product yield and product property data are listed in table 5.

The difference is that in the hydrocracking reaction zone of comparative example 5, the loading volume ratio of the hydrocracking catalyst I, the hydrocracking catalyst II and the hydrocracking catalyst III was 40: 35: 25.

comparative example 6 in the hydrocracking reaction zone, the packing volume ratio of the hydrocracking catalyst I, the hydrocracking catalyst II, and the hydrocracking catalyst III was 15: 35: 50.

example 6 in the hydrocracking reaction zone, the packing volume ratio of the hydrocracking catalyst I, the hydrocracking catalyst II and the hydrocracking catalyst III was 20: 55: 25.

example 7 in the hydrocracking reaction zone, the packing volume ratio of the hydrocracking catalyst I, the hydrocracking catalyst II and the hydrocracking catalyst III was 30: 45: 25.

as can be seen from the data in table 5, the yields of the product heavy naphtha and jet fuel components were 34.36% and 35.34%, respectively, using a high volume fraction of hydrocracking catalyst I in the hydrocracking catalyst staging scheme of comparative example 5 at the same conversion.

Comparative example 6 hydrocracking catalyst grading scheme using a high volume fraction of hydrocracking catalyst III, the yields of product heavy naphtha and jet fuel were 32.34% and 39.85%, respectively.

Example 6 yields of product heavy naphtha and jet fuel components were 34.65% and 41.87%, respectively, using the preferred hydrocracking catalyst staging scheme of the present invention.

Example 7 yields of product heavy naphtha and jet fuel components were 36.33% and 40.94%, respectively, using the preferred hydrocracking catalyst staging scheme of the present invention.

Therefore, when the method provided by the invention is adopted, the yield of the heavy naphtha and jet fuel components is high, the selectivity is good, the reaction activity and the stability of the hydrofining and hydrocracking catalyst are matched well, and the overall operation stability of the device is good.

TABLE 1 Properties of the raw materials

TABLE 2

TABLE 3

TABLE 4

TABLE 5

Claims

1. A hydrocracking method is characterized in that raw oil and hydrogen are mixed and then sequentially pass through a hydrofining reaction zone and a hydrocracking reaction zone, reaction products are obtained and separated to obtain heavy naphtha, jet fuel components and tail oil,

the conversion rate of raw materials is controlled to be 79-92%, and the conversion rate of the raw materials is defined as: the conversion rate of the raw material is 100 percent and the yield of the tail oil; the distillation range of tail oil is more than 282 ℃;

the volume of the total catalyst in the hydrocracking reaction zone is 100 percent, the volume fraction of the hydrocracking catalyst I is 15 to 35 percent, the volume fraction of the hydrocracking catalyst II is 35 to 65 percent, and the volume fraction of the hydrocracking catalyst III is 20 to 40 percent;

the content of the active metal oxide in the hydrocracking catalyst II is the same as that of the active metal oxide in the hydrocracking catalyst III and is 4-8% higher than that of the active metal oxide in the hydrocracking catalyst I; the content of the Y-type molecular sieve in the carrier of the hydrocracking catalyst I is the same as that of the Y-type molecular sieve in the carrier of the hydrocracking catalyst II, and is 1.8-2.5 times of that of the Y-type molecular sieve in the carrier of the hydrocracking catalyst III.

2. The method according to claim 1, wherein the distillation range of the feedstock oil is 200 ℃ to 580 ℃, the mass fraction of sulfur is 0.2% to 2.5%, and the mass fraction of nitrogen is 700 μ g/g to 3000 μ g/g.

3. The method according to claim 1 or 2, wherein the raw oil is selected from vacuum wax oils having a paraffin mass fraction of 1% to 28%.

4. The method according to claim 3, wherein the raw oil is selected from naphthenic base or intermediate base vacuum wax oil with paraffin mass fraction of 1-20%.

5. The method according to claim 1 or 2, wherein the raw material oil is a mixed raw material of vacuum wax oil and one or more selected from deasphalted oil, coal tar, direct and indirect coal liquefaction oil and catalytic cracking light cycle oil, wherein the mass fraction of the vacuum wax oil is 75-99%, and the mass fraction of paraffin of the mixed raw material is 1-28%.

6. The method of claim 5, wherein the mixed feedstock has a paraffin mass fraction of 1% to 20%.

7. The process of claim 1, wherein the feedstock conversion is in the range of 82% to 88%.

8. The process of claim 1, wherein the hydrofinishing reaction conditions are: the hydrogen partial pressure is 6.0MPa to 20.0MPa, the reaction temperature is 280 ℃ to 400 ℃, and the liquid hourly space velocity is 0.5h^-1～6h^-1The volume ratio of hydrogen to oil is 300-2000.

9. The process of claim 1, wherein the hydrocracking reaction conditions are: hydrogen partial pressure of 6.0MPa-20.0 MPa, reaction temperature of 290-420 ℃, and liquid hourly space velocity of 0.3h^-1～5h^-1The volume ratio of hydrogen to oil is 300-2000.

10. The process of claim 1 wherein the hydrofinishing catalyst is at least one non-noble group VIB metal, or at least one non-noble group VIII metal, or a combination thereof, supported on alumina and/or silica-alumina.

11. The process of claim 10 wherein said group VIII non-noble metal is selected from the group consisting of nickel and/or cobalt, said group VIB non-noble metal is selected from the group consisting of molybdenum and/or tungsten, and wherein the total content of said nickel and/or cobalt as oxides is from 1 wt% to 15 wt%, the total content of said molybdenum and/or tungsten as oxides is from 5 wt% to 40 wt%, and the balance is a support, based on the total weight of said hydrofinishing catalyst.

12. The process according to claim 1, wherein in the hydrocracking catalyst I, the heat-resistant inorganic oxide is one or more selected from silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from metals in a VIB group and a VIII group; based on the hydrocracking catalyst I as a whole, calculated by oxides, 14-30 wt% of VIB group metal, 2-8 wt% of VIII group metal and the balance of carrier;

based on the carrier, the Y-type molecular sieve accounts for 40-65 wt%, and the rest is heat-resistant inorganic oxide.

13. The method of claim 12, wherein the Y-type molecular sieve is 40 to 65 wt.%, the alumina is 20 to 40 wt.%, and the amorphous aluminum silicate is 0 to 32 wt.%, based on the support.

14. The process according to claim 1, wherein in the hydrocracking catalyst II, the heat-resistant inorganic oxide is one or more selected from silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from metals in a VIB group and a VIII group; taking the hydrocracking catalyst II as a whole as a reference, wherein the weight percentage of the VIB group metal is 15-33 percent, the weight percentage of the VIII group metal is 2-8 percent, and the balance is a carrier by the weight percentage of oxides;

15. The process according to claim 1, wherein in the hydrocracking catalyst III, the heat-resistant inorganic oxide is one or more selected from silicon oxide, aluminum oxide and amorphous aluminum silicate, and the active metal component is at least two metal components selected from metals in a VIB group and a VIII group; taking the hydrocracking catalyst III as a whole as a reference, wherein the weight percentage of the VIB group metal is 15-33 percent, the weight percentage of the VIII group metal is 2-8 percent, and the balance is a carrier by the weight percentage of oxides;

based on the carrier, the weight of the Y-type molecular sieve is 15-25 percent, and the balance is heat-resistant inorganic oxide.