A hydrocracking process for the production of high octane gasoline blending components in high yield

Abstract

The present application relates to the technical field of hydrocarbon oil conversion, and discloses a hydrocracking method for producing high-octane gasoline blending components, comprising the following steps: introducing light oil into a hydrocracking reaction zone which is sequentially filled with a protective catalyst and a hydrocracking catalyst under low-pressure hydrogen conditions to perform a hydrocracking reaction, so as to obtain a hydrocracking product; the content of saturated hydrocarbons in the light oil is 90wt%-100wt%; and the hydrocracking product is separated; the process method provided by the present application has the advantages of high liquid yield, high content of isomeric alkanes in the product, and very low content of aromatic hydrocarbons.

Description

Technical Field

[0001] This invention relates to the technical field of hydrocarbon oil conversion, and specifically to a hydrocracking method for producing high-octane gasoline blending components. Background Technology

[0002] With the development of the national economy, the market demand for olefins and aromatics is continuously increasing. However, this has also led to an increase in the production of low-value-added light naphtha as a byproduct of refinery chemical production, such as hydrocracking light naphtha and aromatic residue oil. Since these naphtha fractions themselves have low octane numbers, low demand for blended gasoline, and mostly high cycloalkane content, they are not suitable for direct use as feedstock for ethylene cracking. Therefore, such refinery light naphtha urgently needs a processing method to increase its added value.

[0003] Generally speaking, naphtha fractions such as aromatic residue oil have low sulfur and nitrogen content and low demand for refining. If the cycloalkanes in the feedstock are selectively converted into alkanes through shallow hydrocracking, the product can be used as a chemical feedstock or gasoline blending component, while solving the problem of excess low-value-added residue oil resources in refineries.

[0004] CN112409121A discloses a method for converting light naphtha into low-carbon olefins and aromatics. Light naphtha with a C5 and C6 alkane content of 99% undergoes isomerization separation. The isomerized components are fed into a hydrocracking unit and separated to obtain refinery dry gas, propane, n-butane, and isobutane. These components are then further converted into ethylene and propylene through steam cracking or propane dehydrogenation units. The hydrocracking unit conditions include a temperature of 330–360°C and a gauge pressure of 6–8 MPa. After separation in the hydrocracking unit, the proportions of refinery dry gas, propane, n-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 a two-stage reaction zone. The feedstock passes through a first reactor packed with a bifunctional catalyst, where a portion of the light naphtha is reformed into BTEX, and another portion is cracked into ethane, propane, and butane. The effluent from the first reactor is passed into a gas-liquid separation unit to produce liquid and gaseous products. After removing hydrogen and methane from the gaseous products, the gaseous products are passed through a second reactor under steam cracking conditions to convert the gas into low-carbon olefins.

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

[0007] Conventional hydrocracking technology or units primarily process feedstocks such as diesel and wax oil, while their main products include light naphtha, heavy naphtha, jet fuel, diesel, and tail oil. Light naphtha, in particular, has a low octane number, making it unsuitable as a good gasoline blending component. While hydrocracking technologies involving the production of low-carbon alkanes from light oil feedstocks can achieve the goal of isomerizing light oil feedstocks to increase octane number, they mostly require precious metal catalysts or operate under harsh conditions. Summary of the Invention

[0008] The purpose of this invention is to produce naphtha products with higher isohydrocarbon content using low-value-added refinery light oil as raw material under milder conditions, thereby increasing the octane number of the raw material.

[0009] To achieve the above objectives, the present invention provides a hydrocracking method for producing high-octane gasoline blending components, the method comprising:

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

[0011] (2) The hydrocracking product is subjected to gas-liquid separation to obtain a liquid product; the conditions are controlled so that the yield of the liquid product is not less than 88 wt%.

[0012] (3) The liquid product is fractionated to obtain a cracked naphtha product; the isomer selectivity of the cracked naphtha product is above 72%;

[0013] The conditions for the hydrocracking reaction are controlled such that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons with C5 or higher is 1% to 12%; and when the light oil is diesel fraction feedstock, the conversion rate of the >165℃ fraction is 25% to 68%.

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

[0015] Conversion rate of >165℃ fraction = (1 - mass percentage of >165℃ fraction in the liquid product * yield of the liquid product / mass percentage of >165℃ fraction in the light oil) * 100%;

[0016] The hydrocracking catalyst contains an active metal component and a support, and the support contains an acidic component; the acidic component is at least one of β-type molecular sieve and modified β-type molecular sieve, and the content of the acidic component is 20wt% to 45wt% based on the weight of the support.

[0017] The method of the present invention enables the conversion of naphtha feedstock with high cycloalkane content into naphtha product mainly composed of low-carbon isoparaffins under low-pressure hydrogen-exposed conditions. This product (preferably after being processed) can be used as a blending component for high-octane gasoline.

[0018] Furthermore, the process method provided by this invention has the advantages of high liquid yield, high content of isoalkanes in the product, and very low content of aromatics. Attached Figure Description

[0019] Figure 1 This 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.

[0020] Explanation of reference numerals in the attached figures

[0021] Numbers 1, 3, 5, 7, 9, 11, 12, 14, 15, and 16 are all pipelines.

[0022] 2: Raw material oil pump

[0023] 4: Heating furnace

[0024] 6: Hydrocracking Reaction Zone

[0025] 8: High-pressure separator

[0026] 10: Gas purification unit

[0027] 13: Fractionation Unit Detailed Implementation

[0028] The endpoints and any values ​​of the ranges disclosed herein 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 the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0029] As mentioned above, this invention provides a hydrocracking method for producing high-octane gasoline blending components, the method comprising:

[0030] (1) Under low-pressure hydrogenation conditions, light oil is introduced into a hydrocracking reaction zone filled with a hydrocracking catalyst to carry out a hydrocracking reaction to obtain hydrocracking products; the content of saturated hydrocarbons in the light oil is 90wt% to 100wt%, and the light oil is naphtha feedstock or diesel fraction feedstock.

[0031] (2) The hydrocracking product is subjected to gas-liquid separation to obtain a liquid product; the conditions are controlled so that the yield of the liquid product is not less than 88 wt%.

[0032] (3) The liquid product is fractionated to obtain a cracked naphtha product; the isomer selectivity of the cracked naphtha product is above 72%;

[0033] The conditions for the hydrocracking reaction are controlled such that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons with C5 or higher is 1% to 12%; and when the light oil is diesel fraction feedstock, the conversion rate of the >165℃ fraction is 25% to 68%.

[0034] Conversion rate of hydrocarbons with C5 or higher = (1 - mass percentage of hydrocarbons with C5 or higher in the liquid product * yield of the liquid product / mass percentage of hydrocarbons with C5 or higher in the light oil) * 100%;

[0035] Conversion rate of >165℃ fraction = (1 - mass percentage of >165℃ fraction in the liquid product * yield of the liquid product / mass percentage of >165℃ fraction in the light oil) * 100%;

[0036] The hydrocracking catalyst contains an active metal component and a support, and the support contains an acidic component; the acidic component is at least one of β-type molecular sieve and modified β-type molecular sieve, and the content of the acidic component is 20wt% to 45wt% based on the weight of the support.

[0037] The yield of the liquid product is calculated as follows: yield of liquid product = (1 - total mass of gaseous products obtained after gas-liquid separation and fractionation in the hydrocracking products) / mass of the light oil * 100%.

[0038] 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 that of the naphtha feedstock, and more preferably 3-10 units higher.

[0039] The cracked naphtha product of the present invention contains low-carbon isomeric hydrocarbons, preferably C5-C9 isomeric alkanes, including but not limited to 2-methylbutane, 2,2-dimethylpropane, 2,2-dimethylbutane, 2,2,3-trimethylbutane and 2,2,3-trimethylpentane, etc.

[0040] When the light oil is naphtha feedstock, the cracking products of the present invention include cracked gas and cracked naphtha products. The gaseous products include C1-C4 gases, and the liquid products are hydrocarbons of C5 and above.

[0041] When the light oil is a diesel fraction feedstock, the cracking products of the present invention include cracked gas, cracked naphtha products and diesel, wherein the carbon number range of cracked naphtha products and diesel varies depending on the cutting temperature.

[0042] More preferably, the conditions of the hydrocracking reaction are controlled such that the conversion rate of hydrocarbons with C5 or higher is 1% to 8%, or the conversion rate of the >165°C fraction is 25% to 45%.

[0043] The method of the present invention may further include preheating the light oil, either alone or together with hydrogen, before introducing the light oil into the hydrocracking reaction zone for hydrocracking; for example, preheating it in a heating furnace; and then introducing the preheated material into the hydrocracking reaction zone for the hydrocracking reaction. The present invention does not have particular requirements for the preheating temperature; it can be the temperature required for the hydrocracking reaction or slightly lower.

[0044] Preferably, the light oil has a carbon number of C5 to C12.

[0045] In a preferred embodiment, the light oil contains 10 wt% to 50 wt% alkanes, 45 wt% to 90 wt% cycloalkanes, and 0 wt% to 10 wt% aromatics.

[0046] Preferably, the light oil has a density of 0.70-0.85 g / cm³ at 20°C. 3 .

[0047] In a particularly preferred embodiment, the alkanes content in the light oil is 30 wt% to 50 wt%.

[0048] In a particularly preferred embodiment, the cycloalkanes content in the light oil is 48 wt% to 60 wt%.

[0049] Preferably, the light oil is selected from the group consisting of light diesel oil, reforming residue oil, and residue oil from the DCC gasoline hydrotreating unit.

[0050] In a particularly preferred embodiment, the nitrogen content in the light oil is ≤20 μg / g. In this preferred embodiment, a protective catalyst is not required in the method of the present invention.

[0051] Preferably, the pressure of the hydrocracking reaction is ≤8.0 MPa.

[0052] According to a preferred embodiment, the conditions for the hydrocracking reaction are at least: a temperature of 280–420°C, a pressure of 0.2–8.0 MPa, and a volume hourly space velocity of 0.5–20.0 h⁻¹. -1 The standard hydrogen-to-oil volume ratio is 100–2000. More preferably, the hydrocracking reaction conditions at least satisfy the following: temperature 320–400°C, pressure 1.0–5.0 MPa, and volume hourly space velocity (VHSV) 1.0–10.0 h⁻¹. -1 The standard hydrogen-to-oil volume ratio is 200–1000.

[0053] Preferably, based on the total weight of the hydrocracking catalyst, the content of the active metal component, calculated as oxide, is 10 wt% to 50 wt%.

[0054] Preferably, in the hydrocracking catalyst, the active metal element in the active metal component is selected from at least two of Group VIB and Group VIII metal elements.

[0055] Preferably, in the hydrocracking catalyst, the active metal element includes at least one selected from Group VIB metals and at least one selected from Group VIII metals.

[0056] Preferably, based on the total weight of the hydrocracking catalyst, the content of the Group VIB metal element is 5 wt% to 35 wt% and the content of the Group VIII metal element is 1 wt% to 8 wt% (calculated as oxides).

[0057] In a preferred embodiment, the support in the hydrocracking catalyst further contains a heat-resistant inorganic oxide, which is silicon oxide and / or aluminum oxide.

[0058] Preferably, the content of the heat-resistant inorganic oxide is 55wt% to 80wt% based on the weight of the carrier.

[0059] According to a preferred embodiment, a protective catalyst is further packed upstream of the hydrocracking catalyst. Based on the total volume of the catalyst in the hydrocracking reaction zone, the packing volume of the protective catalyst is 1% to 50%, and the packing volume of the hydrocracking catalyst is 50% to 99%.

[0060] In a preferred embodiment, the protective catalyst is selected from at least one of a hydrorefining catalyst, a hydroarsenic removal catalyst, a hydrochlorination catalyst, and a hydrometallurgical catalyst.

[0061] According to a preferred embodiment, the metal content in the light oil is greater than 1 mg / kg, and the protective catalyst is a hydrorefining catalyst.

[0062] In a preferred embodiment, more preferably, the hydrorefining catalyst contains a protective agent support and a protective agent active metal component, wherein the protective agent support is alumina, and the protective agent active metal component contains at least one element selected from Group VIII metals and at least one element selected from Group VIB metals.

[0063] In a preferred embodiment, more preferably, in the hydrorefining catalyst, based on the total weight of the hydroprotectant, 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% (calculated as oxides).

[0064] In a preferred embodiment, more preferably, the protective active metal component in the hydrorefining catalyst contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

[0065] The gas-liquid separation described in this invention can be performed, for example, in a separator (e.g., a high-pressure separator). The gaseous product obtained after the gas-liquid separation can be purified and recycled back to the unit for the hydrocracking reaction. The liquid product obtained after the gas-liquid separation is preferably subjected to further fractionation to obtain the cracked naphtha product.

[0066] The following combination Figure 1 The schematic diagram of the process flow shown provides a preferred embodiment of a hydrocracking method for producing high-octane gasoline blending components according to the present invention. Specifically, the method includes:

[0067] (1) Under low-pressure hydrogen conditions, light oil is introduced into the heating furnace 4 for preheating via pipeline 1, feedstock oil pump 2 and pipeline 3 in sequence, and hydrogen is introduced into the heating furnace 4 via pipeline 16 to obtain preheated material; the preheated material is introduced into the hydrocracking reaction zone 6, which is sequentially filled with protective catalyst and hydrocracking catalyst, via pipeline 5 to carry out hydrocracking reaction to obtain hydrocracking products;

[0068] (2) The hydrocracking products are introduced into the high-pressure separator 8 via pipeline 7 for gas-liquid phase separation; the gas phase flowing out of the high-pressure separator 8 enters the gas purification unit 10 via pipeline 9, and the purified gas can be recycled back to the reaction system as circulating hydrogen via pipeline 11; the liquid phase flowing out of the high-pressure separator 8 enters the fractionation unit 13 via pipeline 12, and the gas phase rich in propane and butane exits the device via pipeline 14 (which can be used as feedstock for steam cracking or dehydrogenation); after fractionation by the fractionation unit, light naphtha containing C5 and above components is drawn out from pipeline 15 (this part of light naphtha can be used as gasoline blending component or steam cracking feedstock).

[0069] The present invention will be described in detail below through examples. In the following examples, unless otherwise specified, the raw materials used are all commercially available products.

[0070] Unless otherwise specified, the following examples all use Figure 1 The process flow shown is as follows.

[0071] The properties of the light oils used are listed in Table 1; the catalysts used are listed in Table 2.

[0072] The catalysts provided below were prepared using methods known in the art or were obtained commercially, for example, by the preparation method provided in the literature with publication number CN112742440A.

[0073] The isomer selectivity of the following cracked naphtha products is defined as: (Isomerized alkanes content in the liquid product / Total amount of normal and isomerized alkanes in the liquid product) * 100%.

[0074] Table 1

[0075] Crude oil / naming Light oil A Light diesel oil B Light oil C Light oil D Raw material oil / types Naphtha raw materials Diesel fraction 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 Alkane content, mass % 49.45 45.4 32.09 88.07 Cycloalkanes with 8 or more carbon atoms, by mass % 11.58 51.3 39.6 1.65 Total cycloalkanes, % by mass 49.73 51.3 52.61 11.67 Aromatics, mass % 0.71 3.3 15.3 0.26 Distillation range (ASTM-D86), °C 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

[0076] Table 2: Catalyst Information

[0077]

[0078] Example 1

[0079] use Figure 1The process flow shown is as follows, and the process parameters involved, including the absence of a protective catalyst in the hydrocracking reaction zone, are listed in Table 3.

[0080] The distribution and properties of the obtained products are listed in Table 4.

[0081] Comparative Example 1

[0082] use Figure 1 The process flow shown is as follows, and the process parameters involved, including the absence of a protective catalyst in the hydrocracking reaction zone, are listed in Table 3.

[0083] The distribution and properties of the obtained products are listed in Table 4.

[0084] Example 2

[0085] use Figure 1 The process flow shown, as well as the protective catalyst set in the hydrocracking reaction zone (the protective catalyst is set upstream of the hydrocracking catalyst), and the related process parameters are listed in Table 3.

[0086] The distribution and properties of the obtained products are listed in Table 4.

[0087] Comparative Example 2

[0088] use Figure 1 The process flow shown, as well as the protective catalyst set in the hydrocracking reaction zone (the protective catalyst is set upstream of the hydrocracking catalyst), and the related process parameters are listed in Table 3.

[0089] The distribution and properties of the obtained products are listed in Table 4.

[0090] Example 3

[0091] use Figure 1 The process flow shown is as follows, and no protective catalyst is set in the hydrocracking reaction zone. The catalyst used is hydrocracking catalyst II. The relevant process parameters and other information are listed in Table 3.

[0092] The distribution and properties of the obtained products are listed in Table 4.

[0093] Example 4

[0094] use Figure 1 The process flow shown is as follows, and the process parameters involved, including the absence of a protective catalyst in the hydrocracking reaction zone, are listed in Table 3.

[0095] The distribution and properties of the obtained products are listed in Table 4.

[0096] Example 5

[0097] use Figure 1The process flow shown is as follows. The protective catalyst set in the hydrocracking reaction zone is hydrocracking catalyst I, and the hydrocracking catalyst used is hydrocracking catalyst III. The process parameters and other information are listed in Table 3.

[0098] The distribution and properties of the obtained products are listed in Table 4.

[0099] Comparative Example 3

[0100] use Figure 1 The process flow shown is as follows, and no protective catalyst is set in the hydrocracking reaction zone. The catalyst used is hydrocracking catalyst III. The relevant process parameters and other information are listed in Table 3.

[0101] The distribution and properties of the obtained products are listed in Table 4.

[0102] Comparative Example 4

[0103] use Figure 1 The process flow shown is as follows, and the process parameters involved, including the absence of a protective catalyst in the hydrocracking reaction zone, are listed in Table 3.

[0104] Table 3

[0105]

[0106]

[0107] The meaning of the conversion rate in the hydrocracking reaction zone in Table 3 is as follows: when light oil is naphtha feedstock, it represents the conversion rate of hydrocarbons with C5 or higher; when light oil is diesel fraction feedstock, it represents the conversion rate of fractions with temperatures above 165℃.

[0108] Table 3 (continued)

[0109]

[0110] The meaning of the conversion rate in the hydrocracking reaction zone in Table 3 is as follows: when light oil is naphtha feedstock, it represents the conversion rate of hydrocarbons with C5 or higher; when light oil is diesel fraction feedstock, it represents the conversion rate of fractions with temperatures above 165℃.

[0111] Table 4

[0112] 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 Hydrocarbons with C5 or higher, by mass % 93.14 / 92.45 / 91.18 Naphtha yield, wt% / 45.8 / 55.65 / Diesel yield, wt% / 50.67 / 39.41 / RON (a type of crumbled naphtha) 77.4 78.2 78.8 76.8 76.2 Isomer selectivity of crumbled naphtha products, % 72.37 74.03 73.59 72.23 73.08

[0113] Table 4 (continued)

[0114] 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 Hydrocarbons with C5 or higher, by mass % 88.53 90.91 80.02 / Naphtha yield, wt% / / / 70.91 Diesel yield, wt% / / / 16.33 RON (a type of crumbled naphtha) 72.9 68.9 67.2 69.2 Isomer selectivity of crumbled naphtha products, % 68.88 71.05 69.34 66.9

[0115] As can be seen from the above results, the method of the present invention enables the conversion of naphtha feedstock with high cycloalkane content into cracked naphtha product mainly composed of low-carbon isoparaffins under low-pressure hydrogen conditions. This product (preferably after cutting) can be used as a blending component for high-octane gasoline.

[0116] Furthermore, the results from Example 5 of this invention show that by using suitable hydrorefining or hydrodemetallizing agents to treat metal-containing feedstocks and meeting the feed requirements of the cracking section, high-quality cracking products can also be obtained. These products are rich in isoparaffins, and the product distribution does not change significantly.

[0117] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within 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) Under low-pressure hydrogenation conditions, light oil is introduced into a hydrocracking reaction zone filled with hydrocracking catalyst to carry out hydrocracking reaction and obtain hydrocracking products; the content of saturated hydrocarbons in the light oil is 90wt%~100wt%, and the light oil is naphtha feedstock or diesel fraction feedstock. (2) The hydrocracking products are subjected to gas-liquid separation to obtain a liquid product; the conditions are controlled such that the yield of the liquid product is not less than 88 wt%. (3) The liquid product is fractionated to obtain cracked naphtha product; the isomer selectivity of the cracked naphtha product is above 72%; The conditions for the hydrocracking reaction are controlled such that when the light oil is naphtha feedstock, the conversion rate of hydrocarbons with C5 or higher is 1% to 12%; and when the light oil is diesel fraction feedstock, the conversion rate of the >165℃ fraction is 25% to 68%. Conversion rate of hydrocarbons with C5 or higher = (1 - mass percentage of hydrocarbons with C5 or higher in the liquid product * yield of the liquid product / mass percentage of hydrocarbons with C5 or higher in the light oil) * 100%; Conversion rate of >165℃ fraction = (1 - mass percentage of >165℃ fraction in the liquid product * yield of the liquid product / mass percentage of >165℃ fraction in the light oil) * 100%; The hydrocracking catalyst contains an active metal component and a support, and the support contains an acidic component; the acidic component is at least one of β-type molecular sieve and modified β-type molecular sieve, and the content of the acidic component is 20wt%~45wt% based on the weight of the support.

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

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

4. The hydrocracking reaction according to claim 1 or 2, wherein, The light oil contains 10wt% to 50wt% alkanes, 45wt% to 90wt% cycloalkanes, and 0wt% to 10wt% aromatics.

5. The hydrocracking method according to claim 1 or 2, wherein, The nitrogen content in the light oil is ≤20 μg / g.

6. The hydrocracking method according to claim 1 or 2, wherein, The conditions for the hydrocracking reaction must at least meet the following requirements: temperature 280~420℃, pressure 0.2~8.0MPa, and feed volume hourly space velocity 0.5~20.0h. -1 The standard hydrogen-to-oil volume ratio is 100-2000.

7. The hydrocracking method according to claim 6, wherein, The conditions for the hydrocracking reaction must at least meet the following requirements: temperature 320~400℃, pressure 1.0~5.0MPa, and feed volume hourly space velocity 1.0~10.0h. -1 The standard hydrogen-to-oil volume ratio is 200-1000.

8. The hydrocracking method according to claim 1 or 2, wherein, Based on the total weight of the hydrocracking catalyst, the content of the active metal component, calculated as oxide, is 10wt% to 50wt%.

9. The hydrocracking method according to claim 1 or 2, wherein, The active metal element in the active metal component is selected from at least two of Group VIB and Group VIII metal elements.

10. The hydrocracking method according to claim 9, wherein, The active metal element includes at least one selected from Group VIB metal elements and at least one selected from Group VIII metal elements.

11. The hydrocracking method according to claim 9, wherein, Based on the total weight of the hydrocracking catalyst, the content of the Group VIB metal element is 5wt% to 35wt% and the content of the Group VIII metal element is 1wt% to 8wt% (calculated as oxides).

12. The hydrocracking method according to claim 1 or 2, wherein, In the hydrocracking catalyst, the support also contains heat-resistant inorganic oxides, which are silicon oxide and / or aluminum oxide.

13. The hydrocracking method according to claim 12, wherein, Based on the weight of the carrier, the content of the heat-resistant inorganic oxide is 55wt%~80wt%.

14. The hydrocracking method according to claim 1 or 2, wherein, Upstream of the hydrocracking catalyst, a protective catalyst is also packed. Based on the total volume of the catalyst in the hydrocracking reaction zone, the packing volume of the protective catalyst is 1% to 50%, and the packing volume of the hydrocracking catalyst is 50% to 99%.

15. The hydrocracking method according to claim 14, wherein, The protective catalyst is selected from hydrorefining catalysts.

16. The hydrocracking method according to claim 14, wherein, The protective catalyst is selected from at least one of the following: hydrodearsenic removal catalyst, hydrodechlorination catalyst, and hydrodemetallization catalyst.

17. The method according to claim 15, wherein, The light oil contains more than 1 mg / kg of metal, and the protective catalyst is a hydrorefining catalyst.

18. The method according to claim 17, wherein, The hydrorefining catalyst contains a protective agent support and a protective agent active metal component. The protective agent support is alumina, and the protective agent active metal component contains at least one element selected from Group VIII metals and at least one element selected from Group VIB metals.

19. The method according to claim 18, wherein, In the hydrorefining catalyst, based on the total weight of the hydrorefining catalyst, the content of the Group VIII metal element is 0.3wt% to 5wt% and the content of the Group VIB metal element is 1wt% to 30wt% (calculated as oxides).

20. The method according to claim 18, wherein, In the hydrorefining catalyst, the active metal component of the protective agent contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

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