Hydrocracking method for increasing yield of high-octane gasoline blending component

Abstract

The present invention relates to the technical field of hydrocarbon oil conversion, and discloses a high octane number gasoline blending component yield increasing hydrocracking method, which comprises: introducing light oil into a hydrocracking reaction zone sequentially filled with a protection catalyst and a hydrocracking catalyst under a low pressure hydrogen condition, and carrying out a hydrocracking reaction to obtain a hydrocracking product; the content of saturated hydrocarbon in the light oil is 90 wt%-100 wt%; and separating the hydrocracking product. The process method provided by the invention has the advantages of high liquid yield, high isoparaffin content of the product and very low aromatic hydrocarbon content.

Description

Technical Field

[0001] The invention relates to the technical field of hydrocarbon oil conversion, and in particular to a hydrocracking method for producing more high-octane gasoline blending components. Background Art

[0002] With the development of the national economy, the market demand for olefins and aromatics continues to increase, but this also leads to an increase in the production of low-value-added light naphtha by-products in the process of producing chemical materials in refineries, such as hydrocracking light naphtha and aromatic raffinate oil. Since these naphtha fractions themselves have low octane numbers, low demand for blending gasoline, and most of them have high cycloparaffin content, they are not suitable for direct use as ethylene cracking raw materials. Therefore, such light oil in refineries urgently needs a treatment method to increase the added value of its products.

[0003] Generally speaking, naphtha fractions such as aromatic raffinate oil have low sulfur and nitrogen contents and do not require high refining requirements. If the cycloalkanes in the raw materials are selectively converted into chain alkanes through shallow hydrocracking, the products can be used as chemical materials or gasoline blending components, while solving the problem of excess low-value-added raffinate oil resources in refineries.

[0004] CN112409121A discloses a method for converting light naphtha into low-carbon olefins and aromatics, wherein light naphtha with a C5 and C6 paraffin content of 99% is separated by normal isomerization, and the isomer components are fed to a hydrocracking unit and separated to obtain refinery dry gas, propane, normal butane and isobutane, and then these components are further converted into ethylene and propylene by steam cracking or propane dehydrogenation. The conditions of the hydrocracking unit in the method include a temperature of 330 to 360°C and a pressure of 6 to 8 MPa gauge pressure. After separation by the hydrocracking unit, the proportions of refinery dry gas, propane, normal butane and isobutane are 6%, 31%, 29% and 34% respectively.

[0005] WO2021236149A1 discloses a method for converting light naphtha fractions into high-value products through two-stage reaction zones. The raw material passes through a first reactor loaded with a bifunctional catalyst, partially reforming the light naphtha into BTEX, and partially cracking the light naphtha into ethane, propane and butane. The effluent from the first reactor is passed through a gas-liquid separation unit to produce liquid and gas products. After removing hydrogen and methane from the gas product, the gas is converted into light olefins under steam cracking conditions through a second reactor.

[0006] WO2022144802A1 discloses a method for maximizing the conversion of normal alkanes into low-carbon normal alkanes, wherein naphtha with a normal alkane content of 40-80% is converted into low-carbon alkanes by hydrocracking, wherein the ratio of isomeric C4 to normal C4 does not exceed 25%. In the method, the catalyst comprises an LTA molecular sieve with a pore size of 0.30 to 0.50 nm and one or more metals selected from Pd, Pt and Au, and the conditions include a temperature of 199 to 427°C, a pressure of 0.69 to 13.79 MPa and a reaction time of 0.1 to 5 h. -1 Mass airspeed.

[0007] The main processing raw materials of conventional hydrocracking technology or hydrocracking unit include diesel and wax oil, and the main products include light naphtha, heavy naphtha, jet fuel, diesel and tail oil, among which the octane number of light naphtha products is low and it is difficult to be a good gasoline blending component. Although the hydrogenation technology involving the production of low-carbon alkanes from light oil raw materials can achieve the purpose of isomerizing light oil raw materials to increase the octane number, most of them must use precious metal catalysts or have relatively harsh operating conditions. Summary of the invention

[0008] The purpose of the present invention is to use the refinery light oil with lower added value as raw material, produce the naphtha product with higher isomeric hydrocarbon content under milder conditions, and improve the octane number of the raw material.

[0009] In order to achieve the above object, the present invention provides a hydrocracking method for producing more high-octane gasoline blending components, the method comprising:

[0010] (1) introducing light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst under low pressure and hydrogen conditions to carry out a hydrocracking reaction to obtain a hydrocracking product; the content of saturated hydrocarbons in the light oil is 90 wt% to 100 wt%, and the light oil is a naphtha feedstock or a diesel fraction feedstock;

[0011] (2) separating the hydrocracking product into gas and liquid to obtain a liquid product; controlling the conditions so that the yield of the liquid product is not less than 88 wt %;

[0012] (3) fractionating the liquid product to obtain a cracked naphtha product; the cracked naphtha product has an isomerization selectivity of more than 72%;

[0013] The conditions of the hydrocracking reaction are controlled so that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons above C5 is 1% to 12%; when the light oil is diesel fraction feedstock, the conversion rate of fractions above 165°C is 25% to 68%;

[0014] Conversion rate of C5 and above hydrocarbons = (1-mass percentage of C5 and above hydrocarbons in the liquid product * yield of the liquid product / mass percentage of C5 and above hydrocarbons in the light oil) * 100%;

[0016] Conversion rate of fractions with a temperature of >165°C = (1-mass percentage of fractions with a temperature of >165°C in the liquid product*yield of the liquid product / mass percentage of fractions with a temperature of >165°C in the light oil)*100%;

[0017] The hydrocracking catalyst contains an active metal component and a carrier, and the carrier contains an acidic component; the acidic component is at least one of a β-type molecular sieve and a modified product of a β-type molecular sieve, and the content of the acidic component is 20wt% to 45wt% based on the weight of the carrier.

[0018] The method of the present invention realizes the conversion of low-nitrogen naphtha raw materials with high cycloalkane content into naphtha products mainly containing low-carbon isomerized paraffins under low-pressure hydrogenation conditions. The product (preferably after cutting) can be used as a high-octane gasoline blending component.

[0019] In addition, the process provided by the present invention has the advantages of high liquid yield, high isoparaffin content in the product and very low aromatic content. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 The present invention is a schematic flow diagram of a hydrocracking method for producing high-octane gasoline blending components according to a preferred embodiment of the present invention.

[0021] Description of Reference Numerals

[0022] 1, 3, 5, 7, 9, 11, 12, 14, 15, 16 are pipelines

[0023] 2: Raw oil pump

[0024] 4: Heating furnace

[0025] 6: Hydrocracking reaction zone

[0026] 8: High pressure separator

[0027] 10: Gas purification unit

[0028] 13: Fractionation unit DETAILED DESCRIPTION

[0029] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0030] As mentioned above, the present invention provides a hydrocracking method for producing more high-octane gasoline blending components, the method comprising:

[0031] (1) introducing light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst under low pressure and hydrogen conditions to carry out a hydrocracking reaction to obtain a hydrocracking product; the content of saturated hydrocarbons in the light oil is 90 wt% to 100 wt%, and the light oil is a naphtha feedstock or a diesel fraction feedstock;

[0032] (2) separating the hydrocracking product into gas and liquid to obtain a liquid product; controlling the conditions so that the yield of the liquid product is not less than 88 wt %;

[0033] (3) fractionating the liquid product to obtain a cracked naphtha product; the cracked naphtha product has an isomerization selectivity of more than 72%;

[0034] The conditions of the hydrocracking reaction are controlled so that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons above C5 is 1% to 12%; when the light oil is diesel fraction feedstock, the conversion rate of fractions above 165°C is 25% to 68%;

[0035] Conversion rate of C5 and above hydrocarbons = (1-mass percentage of C5 and above hydrocarbons in the liquid product * yield of the liquid product / mass percentage of C5 and above hydrocarbons in the light oil) * 100%;

[0036] Conversion rate of fractions with a temperature of >165°C = (1-mass percentage of fractions with a temperature of >165°C in the liquid product*yield of the liquid product / mass percentage of fractions with a temperature of >165°C in the light oil)*100%;

[0037] The hydrocracking catalyst contains an active metal component and a carrier, and the carrier contains an acidic component; the acidic component is at least one of a β-type molecular sieve and a modified product of a β-type molecular sieve, and the content of the acidic component is 20wt% to 45wt% based on the weight of the carrier.

[0038] The yield of the liquid product is calculated as follows: yield of liquid product = (1-total mass of gas products obtained after gas-liquid separation and fractionation in the hydrocracking product) / mass of the light oil*100%.

[0039] The naphtha feedstock and the cracked naphtha product of the present invention are naphthas of different properties. Preferably, the octane number of the cracked naphtha product of the present invention is at least 3 units higher than the octane number of the naphtha feedstock, preferably 3-10 units higher.

[0040] The cracked naphtha product of the present invention contains low-carbon isomerized hydrocarbons, preferably C5-C9 isomerized paraffins, including but not limited to 2-methylbutane, 2,2-dimethylpropane, 2,2-dimethylbutane, 2,2,3-trimethylbutane and 2,2,3-trimethylpentane.

[0041] When the light oil is naphtha feedstock, the cracking products of the present invention include cracked gas and cracked naphtha products, the gas products include C1-C4 gases, and the liquid products are hydrocarbons above C5.

[0042] When the light oil is a diesel fraction feedstock, the cracking products of the present invention include cracked gas, cracked naphtha products and diesel. In this case, the carbon number ranges of the cracked naphtha products and diesel are different according to the cutting temperature.

[0043] More preferably, the conditions of the hydrocracking reaction are controlled so that the conversion rate of hydrocarbons above C5 is 1% to 8%, or the conversion rate of the fraction >165°C is 25% to 45%.

[0044] The method of the present invention may also include, before introducing the light oil into the hydrocracking reaction zone for the hydrocracking reaction, preheating the light oil alone or together with hydrogen, for example, introducing the light oil into a heating furnace for preheating treatment; and then introducing the preheated material into the hydrocracking reaction zone for the hydrocracking reaction. The present invention has no special requirements for the preheating temperature, which may be the temperature required for the hydrocracking reaction or slightly lower than the temperature required for the hydrocracking reaction.

[0045] Preferably, the carbon number of the light oil is C5 to C12.

[0046] Preferably, the light oil contains 10 wt% to 50 wt% of paraffins, 45 wt% to 90 wt% of cycloparaffins, and 0 wt% to 10 wt% of aromatics.

[0047] Preferably, the density of the light oil at 20°C is 0.70-0.85 g / cm 3 .

[0048] In a particularly preferred case, the paraffin content in the light oil is 30 wt% to 50 wt%.

[0049] In a particularly preferred case, the cycloalkane content in the light oil is 48 wt% to 60 wt%.

[0050] Preferably, the light oil is selected from the group consisting of light diesel, reforming raffinate, and DCC gasoline hydrogenation unit raffinate.

[0051] In a particularly preferred case, the nitrogen content in the light oil is ≯20 μg / g. In this preferred case, it is not necessary to use a protected catalyst in the method of the present invention.

[0052] Preferably, the pressure of the hydrocracking reaction is ≯8.0 MPa.

[0053] According to a preferred embodiment, the conditions of the hydrocracking reaction at least meet the following requirements: temperature of 280-420°C, pressure of 0.2-8.0 MPa, volume space velocity of 0.5-20.0 h -1 , the standard hydrogen-to-oil volume ratio is 100-2000. More preferably, the conditions of the hydrocracking reaction at least meet the following conditions: temperature of 320-400°C, pressure of 1.0-5.0 MPa, volume space velocity of 1.0-10.0 h -1 The standard hydrogen-to-oil volume ratio is 200-1000.

[0054] Preferably, based on the total weight of the hydrocracking catalyst, the content of the active metal component in terms of oxide is 10 wt% to 50 wt%.

[0055] Preferably, in the hydrocracking catalyst, the active metal elements in the active metal component are selected from at least two of Group VIB metal elements and Group VIII metal elements.

[0056] Preferably, in the hydrocracking catalyst, the active metal element includes at least one selected from Group VIB metal elements and at least one selected from Group VIII metal elements.

[0057] Preferably, based on the total weight of the hydrocracking catalyst, the content of the VIB group metal element is 5wt% to 35wt% and the content of the VIII group metal element is 1wt% to 8wt% in terms of oxide.

[0058] Preferably, in the hydrocracking catalyst, the carrier further contains a heat-resistant inorganic oxide, and the heat-resistant inorganic oxide is silicon oxide and / or aluminum oxide.

[0059] Preferably, based on the weight of the carrier, the content of the heat-resistant inorganic oxide is 55 wt% to 80 wt%.

[0060] According to a preferred specific embodiment, a protective catalyst is also loaded upstream of the hydrocracking catalyst. Based on the total volume of the catalyst in the hydrocracking reaction zone, the loading volume of the protective catalyst is 1% to 50%, and the loading volume of the hydrocracking catalyst is 50% to 99%.

[0061] Preferably, the protective catalyst is selected from at least one of a hydrotreating catalyst, a hydroarsenic removal catalyst, a hydrodechlorination catalyst and a hydrodemetallization catalyst.

[0062] According to a preferred specific embodiment, the metal content in the light oil is greater than 1 mg / kg, and the protected catalyst is a hydrorefining catalyst.

[0063] In a preferred embodiment, more preferably, the hydrotreating catalyst contains a protectant carrier and a protectant active metal component, the protectant carrier is alumina, and the protectant active metal component contains at least one element selected from Group VIII metal elements and at least one element selected from Group VIB metal elements.

[0064] In a preferred embodiment, more preferably, in the hydrotreating catalyst, based on the total weight of the hydrogenation protective agent, the content of the Group VIII metal element is 0.3 wt% to 5 wt%, and the content of the Group VIB metal element is 1 wt% to 30 wt% in terms of oxide.

[0065] In a preferred embodiment, more preferably, in the hydrotreating catalyst, the protective agent active metal component contains at least one of nickel and cobalt, and contains at least one of molybdenum and tungsten.

[0066] The gas-liquid separation of the present invention can be carried out in a separator (e.g., a high-pressure separator) for example. The gas product obtained after the gas-liquid separation can be recycled back to the device for the hydrocracking reaction after purification. The liquid product obtained after the gas-liquid separation is preferably further fractionated to obtain the cracked naphtha product.

[0067] The following combination Figure 1 The process flow diagram shown provides a preferred specific embodiment of a hydrocracking method for producing high-octane gasoline blending components of the present invention. Specifically, the method comprises:

[0068] (1) Under low-pressure hydrogen conditions, light oil is introduced into a heating furnace 4 through pipeline 1, a feed oil pump 2 and a pipeline 3 in sequence for preheating, and hydrogen is introduced into the heating furnace 4 through pipeline 16 to obtain preheated materials; the preheated materials are introduced into a hydrocracking reaction zone 6 filled with a protective catalyst and a hydrocracking catalyst in sequence through pipeline 5 for hydrocracking reaction to obtain hydrocracking products;

[0069] (2) The hydrocracking product is introduced into a high-pressure separator 8 via pipeline 7 for gas-liquid phase separation; the gas phase flowing out of the high-pressure separator 8 enters a gas purification unit 10 via pipeline 9, and the purified gas can be circulated back to the reaction system as circulating hydrogen via pipeline 11; the liquid phase flowing out of the high-pressure separator 8 enters a fractionation unit 13 via pipeline 12, and the gas phase rich in propane and butane exits the device via pipeline 14 (can be used as a raw material for a steam cracking or dehydrogenation device); after fractionation in the fractionation unit, light naphtha containing components of C5 and above is drawn out from pipeline 15 (this part of light naphtha can be used as a gasoline blending component or a steam cracking raw material).

[0070] The present invention will be described in detail below by way of examples. In the following examples, unless otherwise specified, the raw materials used are all common commercially available products.

[0071] Unless otherwise specified, the following examples use Figure 1 The process flow shown is carried out.

[0072] The properties of the light oil used below are listed in Table 1; the properties of the catalyst used are listed in Table 2.

[0073] The catalysts provided below are all prepared by methods known in the art or commercially available, for example, they can be obtained by the preparation method provided in the document with publication number CN112742440A.

[0074] The isomerization selectivity of the following cracked naphtha products is defined as: (content of isomerized paraffins in the liquid product / total amount of normal and isomerized paraffins in the liquid product)*100%.

[0075] Table 1

[0076] Raw oil / name Light oil A Light diesel B Light oil C Light oil D Raw oil / type Naphtha Raw Materials Diesel Distillate Feedstock Naphtha Raw Materials Naphtha Raw Materials <![CDATA[Density (20 °C) / (g / cm 3 )]]> 0.7106 0.8199 0.7687 0.6908 N mass fraction / (μg / g) 0.4 250 0.3 0.3 S mass fraction / (μg / g) 0.3 325 0.3 0.3 As mass fraction / (μg / g) <0.1 <0.1 <0.1 1.4 Paraffin content, mass % 49.45 45.4 32.09 88.07 C8 and above cycloalkanes, mass % 11.58 51.3 39.6 1.65 Total cycloalkanes, mass % 49.73 51.3 52.61 11.67 Aromatics, mass% 0.71 3.3 15.3 0.26 Distillation range (ASTM-D86), ℃ IBP 59 182 94 49 10％ 64 226 109 56 50％ 78 281 133 71 90％ 117 320 164 101 FBP 147 334 186 129

[0077] Table 2: Catalyst conditions

[0078]

[0079] Example 1

[0080] use Figure 1The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The process parameters and other information involved are listed in Table 3.

[0081] The distribution and properties of the obtained products are listed in Table 4.

[0082] Comparative Example 1

[0083] use Figure 1 The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The process parameters and other information involved are listed in Table 3.

[0084] The distribution and properties of the obtained products are listed in Table 4.

[0085] Example 2

[0086] use Figure 1 The process flow shown is carried out, and a protective catalyst is set in the hydrocracking reaction zone (the protective catalyst is set upstream of the hydrocracking catalyst). The process parameters and other information involved are listed in Table 3.

[0087] The distribution and properties of the obtained products are listed in Table 4.

[0088] Comparative Example 2

[0089] use Figure 1 The process flow shown is carried out, and a protective catalyst is set in the hydrocracking reaction zone (the protective catalyst is set upstream of the hydrocracking catalyst). The process parameters and other information involved are listed in Table 3.

[0090] The distribution and properties of the obtained products are listed in Table 4.

[0091] Example 3

[0092] use Figure 1 The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The catalyst used is hydrocracking catalyst II. The process parameters and other information involved are listed in Table 3.

[0093] The distribution and properties of the obtained products are listed in Table 4.

[0094] Example 4

[0095] use Figure 1 The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The process parameters and other information involved are listed in Table 3.

[0096] The distribution and properties of the obtained products are listed in Table 4.

[0097] Example 5

[0098] use Figure 1The process flow shown in the figure is carried out, the protective catalyst arranged in the hydrocracking reaction zone is the hydrodearsenification catalyst I, the applied hydrocracking catalyst is the hydrocracking catalyst III, and the process parameters and other information involved are listed in Table 3.

[0099] The distribution and properties of the obtained products are listed in Table 4.

[0100] Comparative Example 3

[0101] use Figure 1 The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The catalyst used is hydrocracking catalyst III. The process parameters and other information involved are listed in Table 3.

[0102] The distribution and properties of the obtained products are listed in Table 4.

[0103] Comparative Example 4

[0104] use Figure 1 The process flow shown is carried out, and no protective catalyst is set in the hydrocracking reaction zone. The process parameters and other information involved are listed in Table 3.

[0105] Table 3

[0106]

[0107]

[0108] The conversion rate of the hydrocracking reaction zone in Table 3 means: when the light oil is naphtha raw material, it means the conversion rate of hydrocarbons above C5; when the light oil is diesel fraction raw material, it means the conversion rate of fractions >165°C.

[0109] Table 3 (Continued)

[0110]

[0111] The conversion rate of the hydrocracking reaction zone in Table 3 means: when the light oil is naphtha raw material, it means the conversion rate of hydrocarbons above C5; when the light oil is diesel fraction raw material, it means the conversion rate of fractions >165°C.

[0112] Table 4

[0113] Example 1 Example 2 Example 3 Example 4 Example 5 C1, mass% 0.11 0.09 0.16 0.08 0.22 C2, mass% 0.16 0.21 0.23 0.27 0.37 C3, mass% 1.53 1.17 1.48 1.86 1.74 C4, mass% 5.06 2.06 5.68 2.73 6.49 C5 and above hydrocarbons, mass% 93.14 / 92.45 / 91.18 Naphtha yield, wt% / 45.8 / 55.65 / Diesel yield, wt% / 50.67 / 39.41 / Cracking naphtha product RON 77.4 78.2 78.8 76.8 76.2 Isomerization selectivity of cracked naphtha products, % 72.37 74.03 73.59 72.23 73.08

[0114] Table 4 (Continued)

[0115] Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 C1, mass% 0.08 0.13 0.17 0.23 C2, mass% 0.79 0.23 0.35 0.49 C3, mass% 3.16 1.89 3.87 3.3 C4, mass% 7.44 6.84 15.59 8.74 C5 and above hydrocarbons, mass% 88.53 90.91 80.02 / Naphtha yield, wt% / / / 70.91 Diesel yield, wt% / / / 16.33 Cracking naphtha product RON 72.9 68.9 67.2 69.2 Isomerization selectivity of cracked naphtha products, % 68.88 71.05 69.34 66.9

[0116] From the above results, it can be seen that the method of the present invention realizes the conversion of low-nitrogen naphtha feedstock with a high cycloalkane content into a cracked naphtha product mainly composed of low-carbon isomerized paraffins under low-pressure hydrogenation conditions. This product (preferably after cutting) can be used as a high-octane gasoline blending component.

[0117] In addition, it can be seen from the results of Example 5 of the present invention that by using a suitable hydrotreating or hydrodemetallizing agent to treat the metal-containing raw material and meeting the feed requirements of the cracking stage, high-quality cracking products can also be obtained. The products are rich in isoparaffins and the product distribution does not change much.

[0118] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A hydrocracking method for producing high-octane gasoline blending components, characterized in that: The method includes: (1) introducing light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst under low pressure and hydrogen conditions to carry out a hydrocracking reaction to obtain a hydrocracking product; the content of saturated hydrocarbons in the light oil is 90 wt% to 100 wt%, and the light oil is a naphtha feedstock or a diesel fraction feedstock; (2) separating the hydrocracking product into gas and liquid to obtain a liquid product; controlling the conditions so that the yield of the liquid product is not less than 88 wt %; (3) fractionating the liquid product to obtain a cracked naphtha product; the cracked naphtha product has an isomerization selectivity of more than 72%; The conditions of the hydrocracking reaction are controlled so that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons above C5 is 1% to 12%; when the light oil is diesel fraction feedstock, the conversion rate of fractions above 165°C is 25% to 68%; Conversion rate of C5 and above hydrocarbons = (1-mass percentage of C5 and above hydrocarbons in the liquid product * yield of the liquid product / mass percentage of C5 and above hydrocarbons in the light oil) * 100%; Conversion rate of fractions with a temperature of >165°C = (1-mass percentage of fractions with a temperature of >165°C in the liquid product*yield of the liquid product / mass percentage of fractions with a temperature of >165°C in the light oil)*100%; The hydrocracking catalyst contains an active metal component and a carrier, and the carrier contains an acidic component; the acidic component is at least one of a β-type molecular sieve and a modified product of a β-type molecular sieve, and the content of the acidic component is 20wt% to 45wt% based on the weight of the carrier.

2. The hydrocracking method according to claim 1, wherein: The conditions of the hydrocracking reaction are controlled so that the conversion rate of hydrocarbons above C5 is 1% to 8%, or the conversion rate of the fraction >165°C is 25% to 45%.

3. The hydrocracking method according to claim 1 or 2, wherein: The carbon number of the light oil is C5 to C20.

4. The hydrocracking reaction according to any one of claims 1 to 3, wherein: The light oil contains 10 wt% to 50 wt% of paraffins, 45 wt% to 90 wt% of cycloparaffins, and 0 wt% to 10 wt% of aromatics.

5. The hydrocracking reaction according to any one of claims 1 to 4, wherein: The light oil is selected from the group consisting of light diesel, reforming raffinate, and DCC gasoline hydrogenation unit raffinate.

6. The hydrocracking method according to any one of claims 1 to 5, wherein: The nitrogen content in the light oil is ≯20 μg / g.

7. The hydrocracking method according to any one of claims 1 to 6, wherein: The conditions of the hydrocracking reaction at least meet the following requirements: temperature of 280-420°C, pressure of 0.2-8.0 MPa, feed volume space velocity of 0.5-20.0 h -1 The standard hydrogen-to-oil volume ratio is 100-2000.

8. The hydrocracking method according to claim 7, wherein: The conditions of the hydrocracking reaction at least meet the following requirements: temperature of 320-400°C, pressure of 1.0-5.0 MPa, volume space velocity of 1.0-10.0 h -1 The standard hydrogen-to-oil volume ratio is 200-1000.

9. The hydrocracking method according to any one of claims 1 to 8, wherein: Based on the total weight of the hydrocracking catalyst, the content of the active metal component in terms of oxide is 10 wt% to 50 wt%; Preferably, the active metal elements in the active metal component are selected from at least two of Group VIB metal elements and Group VIII metal elements; Preferably, the active metal element includes at least one selected from the metal elements of Group VIB and at least one selected from the metal elements of Group VIII; Preferably, based on the total weight of the hydrocracking catalyst, the content of the VIB group metal element is 5wt% to 35wt% and the content of the VIII group metal element is 1wt% to 8wt% in terms of oxide.

10. The hydrocracking method according to any one of claims 1 to 9, wherein: In the hydrocracking catalyst, the carrier further contains a heat-resistant inorganic oxide, and the heat-resistant inorganic oxide is silicon oxide and / or aluminum oxide; Preferably, based on the weight of the carrier, the content of the heat-resistant inorganic oxide is 55 wt% to 80 wt%.

11. The hydrocracking method according to any one of claims 1 to 10, wherein: A protection catalyst is also loaded upstream of the hydrocracking catalyst. Based on the total volume of the catalyst in the hydrocracking reaction zone, the loading volume of the protection catalyst is 1% to 50%, and the loading volume of the hydrocracking catalyst is 50% to 99%.

12. The hydrocracking method according to claim 11, wherein: The protective catalyst is selected from at least one of a hydrotreating catalyst, a hydrodearsenification catalyst, a hydrodechlorination catalyst and a hydrodemetallization catalyst.

13. The method according to claim 12, wherein: The metal content in the light oil is greater than 1 mg / kg, and the protected catalyst is a hydrorefining catalyst; Preferably, the hydrotreating catalyst contains a protective agent carrier and a protective agent active metal component, the protective agent carrier is alumina, and the protective agent active metal component contains at least one element selected from Group VIII metal elements and at least one element selected from Group VIB metal elements; Preferably, in the hydrotreating catalyst, based on the total weight of the hydrogenation protective agent, the content of the metal element of Group VIII is 0.3wt% to 5wt%, and the content of the metal element of Group VIB is 1wt% to 30wt% in terms of oxide; Preferably, in the hydrotreating catalyst, the protective agent active metal component contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

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