A hydrocracking process for producing olefinic stocks from light oils

Abstract

The present application relates to the field of hydrocarbon oil conversion and utilization, and discloses a hydrocracking method for producing olefin material from light oil, comprising: introducing raw oil I and raw oil II into a hydrocracking reactor I filled with a hydrocracking catalyst I and a hydrocracking reactor II filled with a hydrocracking catalyst II respectively under low-pressure hydrogen-adjacent conditions to carry out a hydrocracking reaction, so as to obtain hydrocracking product I and hydrocracking product II respectively; and separating the hydrocracking product I and the hydrocracking product II to obtain C3 / C4 product and C5 and above light naphtha product. The method can convert lower-value light oil (such as naphtha fraction) into a raw material suitable for olefin material product under low-pressure hydrogen-adjacent conditions.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of hydrocarbon oil conversion and utilization, in particular to a hydrocracking method for producing olefin material from light oil. BACKGROUND

[0002] The continuous development of the national economy brings about the continuous growth of the demand for chemical products, and the demand for chemical raw materials also grows.

[0003] At present, the production capacity of propane dehydrogenation devices in China has reached 9.9 million tons / year, and the production capacity of ethylene devices has reached nearly 42 million tons / year. In recent years, the production of new ethylene and propane dehydrogenation devices in China has also brought about the rapid growth of demand for chemical light oil and imported propane and butane, and the current import dependence of propane and butane in China is as high as 70%. There is a very broad market in the production of such raw materials.

[0004] In addition, with the impact of new energy such as electric energy, solar energy and hydrogen energy, the demand for fuel oil gradually peaks, and the demand for gasoline blending decreases. Refinery light oil represented by straight-run naphtha, reforming raffinate and coking naphtha is in a situation of resource surplus. In particular, C5, C6 light hydrocarbons and light naphtha products are generally difficult to utilize due to their low aromatic potential and octane value, and therefore it is of great significance to convert these low-value naphtha fractions into high-quality chemical light hydrocarbons through hydrocracking to improve the added value of oil products.

[0005] CN106062148A discloses a process for converting hydrocarbons into olefins, in which hydrocarbon feedstocks represented by naphtha are separated into multiple streams classified by carbon number through a hydrocracking unit, and suitable streams are fed into subsequent steam cracking, propane dehydrogenation and butane dehydrogenation units to produce olefins. The conditions of the hydrocracking unit in the method include a temperature of 470-550℃, a pressure of 0.6-3.0 MPa gauge, and a mass space velocity of 0.2-10 h -1 .

[0006] CN12409121A discloses a method for converting light naphtha into low-carbon olefins and aromatic hydrocarbons, in which light naphtha with a C5, C6 paraffin content of 99% is subjected to normal and isomer separation, the isomer component is fed into a hydrocracking unit and separated to obtain refinery dry gas, propane, n-butane and isobutane, and these components are further converted into ethylene and propylene through steam cracking or propane dehydrogenation units. The conditions of the hydrocracking unit in the method include a temperature of 330-360℃ and a pressure of 6-8 MPa gauge. After separation through the hydrocracking unit, the proportions of refinery dry gas, propane, n-butane and isobutane are 6%, 31%, 29% and 34%, respectively.

[0007] WO2019162392A1 discloses a method for catalytically converting paraffins and naphthenes of a naphtha feedstock into propane by hydrocracking, the naphtha feedstock free of olefins is mixed with hydrogen and subjected to a hydrocracking reaction on a bifunctional catalyst at a temperature of 200-600°C, a pressure of 1-10 MPa, a feed mass hourly space velocity of 0.1-10.0 h -1 and a hydrogen to oil molar ratio of 1-1000, the catalyst used contains one or more of ZSM, MEL or SAPO type molecular sieves having an acidic 10-membered ring channel.

[0008] CN113736516A discloses a treatment process for producing an ethylene raw material from naphtha, the naphtha fraction is mixed with hydrogen and introduced into a liquid phase hydrogenation reactor, the product after hydrogenation is separated by a fractionating column, the gas separated from the top of the column is used as fuel gas, and the qualified naphtha obtained from the bottom of the column is used as an ethylene raw material. The method is a hydrofining process for naphtha, the reaction pressure in the liquid phase hydrogenation reactor is 2.0-6.0 MPa, the reaction temperature is 70-200°C, the liquid volume hourly space velocity is 1-6 / hour, and the chemical hydrogen consumption is 0.2-1.0 wt%.

[0009] The current technology for producing an ethylene raw material from naphtha with relatively low added value generally has harsh reaction conditions, such as the necessity of applying a pressure exceeding 8 MPa and a temperature exceeding 400°C. Secondly, the ideal light hydrocarbon yield of products such as propane, n-butane and n-pentane obtained under relatively mild conditions is low. SUMMARY

[0010] The purpose of the present application is to convert a light oil with relatively low added value (such as a naphtha fraction) into high-quality light hydrocarbons suitable for use as an olefin plant raw material under low-pressure hydrogenation conditions.

[0011] In order to achieve the above-mentioned purpose, the present application provides a hydrocracking method for producing an olefin material from a light oil, which is carried out in a system containing a hydrocracking reactor I and a hydrocracking reactor II arranged in parallel, comprising:

[0012] (1) under low-pressure hydrogenation conditions, introducing a raw oil I and a raw oil II into the hydrocracking reactor I filled with a hydrocracking catalyst I and the hydrocracking reactor II filled with a hydrocracking catalyst II, respectively, to carry out a hydrocracking reaction, and obtaining a hydrocracking product I and a hydrocracking product II, respectively;

[0013] (2) separating the hydrocracking product I and the hydrocracking product II to obtain a C3 / C4 product and a C5 and above light naphtha product;

[0014] The raw oil I and the raw oil II are each independently selected from at least one of light oils; the naphthene content in the raw oil I is 40wt%-100wt%, the total saturated hydrocarbon content is ≧70wt%; the naphthene content in the raw oil II is 0wt%-40wt%, the total saturated hydrocarbon content is ≧70wt%;

[0015] The conditions of the hydrocracking reaction are controlled so that the conversion rate I of the raw oil I is 38%-95%, and the conversion rate II of the raw oil II is 42%-96%;

[0016] The conversion rate I=(1-mass percentage content of C5+ hydrocarbons in the liquid product of the hydrocracking product of the hydrocracking reactor I*yield of the liquid product of the hydrocracking product of the hydrocracking reactor I / mass percentage content of C5+ hydrocarbons in the raw oil I)*100%; and the conversion rate II=(1-mass percentage content of C5+ hydrocarbons in the liquid product of the hydrocracking product of the hydrocracking reactor II*yield of the liquid product of the hydrocracking product of the hydrocracking reactor II / mass percentage content of C5+ hydrocarbons in the raw oil II)*100%.

[0017] The hydrocracking catalyst I and the hydrocracking catalyst II are different, and the hydrocracking catalyst II contains at least one of ZSM type molecular sieve and a modified product of ZSM type molecular sieve as an acidic component.

[0018] The method of the present application can convert low-value light oils (such as naphtha fraction) into a raw material suitable for olefin production under low-pressure hydrogen conditions, for example, can produce propane, n-butane and a small amount of light naphtha rich in low-carbon hydrocarbons under low-pressure hydrogen conditions.

[0019] Using the treatment method provided by the present application, the activity and stability of the hydrocracking catalyst can be considered, and low-value light oils (such as naphtha) can be converted into propane-rich gas products at a high conversion rate. Further, according to the preferred method, according to the naphthene content of the raw material, the method of the present application can be converted in different hydrocracking reaction zones to realize the high-value utilization of naphthene and paraffin in the raw material, and conversion to propane and low-carbon paraffin. BRIEF DESCRIPTION OF DRAWINGS

[0020] Figure 1 is a process flow diagram of a preferred embodiment of the hydrocracking method for producing olefin materials from light oils of the present application.

[0021] REFERENCE SIGNS

[0022] 1, 3, 5, 7, 9, 10, 13, 14, 15, 17, 19, 20, 22, 23, 24 are all pipelines

[0023] 2, 6 are raw oil pumps

[0024] 4, 8 are heating furnaces

[0025] 11, 12 are cracking reaction zones

[0026] 16 is a high-pressure separator

[0027] 18 is a gas purification unit

[0028] 21 is a fractionation unit DETAILED DESCRIPTION

[0029] The endpoints of the ranges and any values disclosed herein are not limited to the precise values stated. The endpoints of the ranges and any values are provided as approximate descriptions of the ranges and are understood to be open-ended. Each range is a continuum of values between the minimum and maximum values of that range, inclusive of the minimum and maximum values. Any smaller sub-ranges within the larger ranges are also specifically disclosed. For values which are deemed to be greater than zero, the value of zero is specifically disclosed as an endpoint. For values which are deemed to be less than one, the value of one is specifically disclosed as an endpoint. For ranges which are deemed to be greater than zero, the value of zero is specifically disclosed as an endpoint of the range. For ranges which are deemed to be less than one, the value one is specifically disclosed as an endpoint of the range. These are but examples of the intended generality of the disclosure. All numerical values are "approximate", meaning that the value of the numerical value can be adjusted to a reasonably equivalent value.

[0030] As previously described, the present application provides a hydrocracking method for producing an olefin feed from a light oil, the method being performed in a system comprising a hydrocracking reactor I and a hydrocracking reactor II connected in parallel, comprising:

[0031] (1) introducing raw oil I and raw oil II into the hydrocracking reactor I packed with a hydrocracking catalyst I and the hydrocracking reactor II packed with a hydrocracking catalyst II, respectively, under low-pressure hydrogen conditions to perform a hydrocracking reaction, to obtain a hydrocracking product I and a hydrocracking product II, respectively;

[0032] (2) separating the hydrocracking product I and the hydrocracking product II to obtain a C3 / C4 product and a C5 and above light naphtha product;

[0033] The raw oil I and the raw oil II are each independently selected from at least one of the light oils; the naphthene content of the raw oil I is 40wt% to 100wt%, the total saturated hydrocarbon content is ≮70wt%; the naphthene content of the raw oil II is 0wt% to 40wt%, the total saturated hydrocarbon content is ≮70wt%;

[0034] The conditions of the hydrocracking reaction are controlled such that the conversion rate I of the raw oil I is 38% to 95%, the conversion rate II of the raw oil II is 42% to 96%;

[0035] The conversion rate I = (1 - mass percentage of C5+ hydrocarbons in the liquid product of the hydrocracking product of the hydrocracking reactor I * yield of the liquid product of the hydrocracking product of the hydrocracking reactor I / mass percentage of C5+ hydrocarbons in the raw oil I) * 100%; the conversion rate II = (1 - mass percentage of C5+ hydrocarbons in the liquid product of the hydrocracking product of the hydrocracking reactor II * yield of the liquid product of the hydrocracking product of the hydrocracking reactor II / mass percentage of C5+ hydrocarbons in the raw oil II) * 100%.

[0036] The hydrocracking catalyst I and the hydrocracking catalyst II are different, and the hydrocracking catalyst II contains at least one of ZSM type molecular sieve and modified product of ZSM type molecular sieve as the acidic component.

[0037] The method of the present application can further comprise, before the raw oil I and the raw oil II are subjected to the hydrocracking reaction, preheating the raw oil. The present application does not have special requirements for the specific operation method of preheating, and the known method in the art can be used. The target temperature of preheating is also not particularly required, and can be equal to or slightly lower than the temperature of the subsequent hydrocracking reaction.

[0038] The present application does not have special requirements for the specific operation of separation, and the person skilled in the art can use the known method in the art. The hydrocracking product I and the hydrocracking product II can be separated respectively, or the hydrocracking product I and the hydrocracking product II can be combined for separation. Exemplarily, after the hydrocracking product I and the hydrocracking product II are mixed, gas-liquid separation is first carried out (for example, in a gas-liquid separator), the gas phase can be returned to the reactor for repeated use as recycle hydrogen, and the liquid phase product can enter the fractionation system for fractionation.

[0039] Preferably, the light oil contains C5-C7 normal hydrocarbons with a content of not more than 30 wt%.

[0040] Preferably, the light oil has a carbon number of C5-C12, and the content of saturated hydrocarbons is 70 wt%-90 wt%.

[0041] Preferably, the dry point of the light oil is not higher than 200℃, the content of paraffin is 30 wt%-100 wt%, and the content of aromatic hydrocarbon is 0 wt%-30 wt%.

[0042] Preferably, the content of naphthenes in the raw oil II is 0.1 wt%-30 wt%.

[0043] According to a preferred specific embodiment, the paraffin content in the raw oil I is 30wt% to 60wt%, and the naphthene content is 40wt% to 70wt%; the paraffin content in the raw oil II is > 80wt%, and the naphthene content is < 20wt%.

[0044] More preferably, the paraffin content in the raw oil I is 40wt% to 55wt%, and the naphthene content is 45wt% to 55wt%.

[0045] Preferably, the light oil is selected from the group consisting of hydrocracked naphtha, ethylene raffinate, reforming raffinate, and DCC gasoline hydrogenation unit raffinate.

[0046] According to a particularly preferred specific embodiment, the nitrogen content in the light oil is < 20μg / g.

[0047] Preferably, the conditions of the hydrocracking reaction independently satisfy: the temperature is 280 to 420℃, the pressure is 0.2 to 8.0MPa, the volume space velocity is 0.1 to 20.0h -1 , and the hydrogen / oil volume ratio is 100 to 2000.

[0048] According to a preferred specific embodiment, the conditions of the hydrocracking reaction in the hydrocracking reactor I satisfy: the temperature is 330 to 420℃, the pressure is 1.0 to 8.0MPa, the volume space velocity is 2.0 to 16.0h -1 , and the hydrogen / oil volume ratio is 500 to 2000.

[0049] According to another preferred specific embodiment, the conditions of the hydrocracking reaction in the hydrocracking reactor II satisfy: the temperature is 280 to 380℃, the pressure is 0.1 to 6.4MPa, the volume space velocity is 0.5 to 16.0h -1 , and the hydrogen / oil volume ratio is 300 to 1000.

[0050] Preferably, the hydrocracking catalyst I and the hydrocracking catalyst II both contain an active metal component and a carrier, and the carrier contains an acidic component; in the hydrocracking catalyst I and the hydrocracking catalyst II, the content of the active metal component, calculated as the oxide, is independently 10wt% to 50wt%.

[0051] Preferably, in the hydrocracking catalyst I and the hydrocracking catalyst II, the active metal element in the active metal component is selected from at least two of the group consisting of the group VIB metal element and the group VIII metal element.

[0052] Preferably, in the hydrocracking catalyst I and the hydrocracking catalyst II, the active metal element includes at least one selected from Group VIB metals and at least one selected from Group VIII metals.

[0053] More preferably, in the hydrocracking catalyst I and the hydrocracking catalyst II, based on the total weight of the hydrocracking catalysts, the content of each Group VIB metal element, calculated as oxides, is independently 5 wt% to 35 wt%, and the content of each Group VIII metal element is independently 1 wt% to 8 wt%.

[0054] According to a preferred embodiment, in both the hydrocracking catalyst I and the hydrocracking catalyst II, the content of the acidic component is independently 45 wt% to 80 wt%, based on the total weight of the support.

[0055] In a preferred embodiment, the acidic component in the hydrocracking catalyst I is at least one of a β-type molecular sieve, a modified product of a β-type molecular sieve, a Y-type molecular sieve, and a modified product of a Y-type molecular sieve.

[0056] Preferably, in both the hydrocracking catalyst I and the hydrocracking catalyst II, the support further contains a heat-resistant inorganic oxide, which is silicon oxide and / or aluminum oxide.

[0057] Preferably, in the hydrocracking catalyst I and the hydrocracking catalyst II, the content of the heat-resistant inorganic oxide is independently 20 wt% to 55 wt%, based on the weight of the support.

[0058] According to a preferred embodiment, based on the total volume of the catalysts in the hydrocracking reactor I and the hydrocracking reactor II, the loading volume of the hydrocracking catalyst I is 30% to 70%, and the loading volume of the hydrocracking catalyst II is 30% to 70%.

[0059] The present invention does not have any particular requirements on the source of the aforementioned catalyst. It can be prepared by methods known in the art, or a commercially available catalyst with corresponding characteristics can be purchased. The present invention will not be described in detail here, and those skilled in the art should not understand it as a limitation of the present invention.

[0060] The following combination Figure 1 The schematic diagram of the process flow illustrates a preferred embodiment of a hydrocracking method for producing olefin feedstock from light oil according to the present invention. Specifically, the method includes:

[0061] The raw oil I from pipeline 1 enters the heating furnace 4 through the raw oil pump 2 and pipeline 3, and is mixed with new hydrogen from pipeline 24; the raw oil II from pipeline 5 enters the heating furnace 8 through the raw oil pump 6 and pipeline 7, and is mixed with new hydrogen from pipeline 24. The raw oil I and the raw oil II are fed into the cracking reaction zone 11 and the cracking reaction zone 12 through pipeline 9 and pipeline 10 respectively, and mainly undergo hydrocracking reactions. The products obtained from the cracking reaction zone 11 and the cracking reaction zone 12 are introduced through pipeline 13 and pipeline 14 respectively, mixed in pipeline 15, and then enter the high-pressure separator 16 for gas-liquid phase separation; the gas phase from the high-pressure separator is introduced into the gas purification unit 18 through pipeline 17, and the purified gas can be used as circulating hydrogen and returned to the reactor through pipeline 19; the liquid phase from the high-pressure separator is introduced into the fractionation unit 21 through pipeline 20, and the gas phase rich in propane obtained in the fractionation unit is introduced out of the device through pipeline 22; the light naphtha containing C5 and above components is introduced out of the device through pipeline 23 after being fractionated in the fractionation unit, and this part of the light naphtha can also be mixed with the raw oil from pipeline 26 according to the production needs, and then circulated to the reaction system for full conversion.

[0062] The present application will be described in detail below by way of examples. In the following examples, the raw materials used are ordinary commercially available products unless otherwise specified.

[0063] In the following examples, the process flow shown in Figure 1 is used unless otherwise specified.

[0064] The properties of the light oil used below are listed in Table 1; the cases of the catalysts used are listed in Table 2.

[0065] The catalysts used in the following examples are prepared by methods known in the art, for example, the method provided in CN112742440A can be used for preparation.

[0066] Table 1: Properties of light oil

[0067] Feed oil Light oil A Light oil B Light oil C Light oil D Density (20°C) / (g / cm 3 )]]> 0.7106 0.6713 0.7249 0.7368 N mass fraction (pg / g) 0.4 <0.3 0.3 11 S mass fraction (pg / g) 0.3 1 0.3 161 Paraffin content, mass % 49.45 91.82 45.15 42.63 Olefins, mass % / / / 13.41 C8+ naphthenes, mass % 11.58 1.25 22.83 5.63 Total naphthenes, mass % 49.73 7.44 34.4 6.67 Aromatics, mass % 0.71 0.27 20.45 37.29 Distillation range (ASTM-D86), °C IBP 59 61 69 35 10％ 64 65 80 48 50％ 78 72 112 103 90％ 117 98 162 174 FBP 147 122 177 199

[0068] Table 2: Cases of catalysts

[0069]

[0070] Example 1

[0071] The process flow shown in Figure 1 is used, and the process parameters and other information involved are listed in Table 3.

[0072] The distribution and properties of the products obtained are listed in Table 4.

[0073] Example 2

[0074] use Figure 1 The process flow shown is as described in Table 3, and the process parameters and other information involved are listed in Table 3.

[0075] The distribution and properties of the obtained products are listed in Table 4.

[0076] Example 3

[0077] use Figure 1 The process flow shown is used to process light oil A and light oil C. The process parameters and other information involved are listed in Table 3.

[0078] The distribution and properties of the obtained products are listed in Table 4.

[0079] Example 4

[0080] use Figure 1 The process flow shown is as described in Table 3, and 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 as described in Table 3, and 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] Comparative Example 2

[0086] use Figure 1 The process flow shown is as described in Table 3, and 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 3

[0089] use Figure 1 The process flow shown is as described in Table 3, and 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] Comparative Example 4

[0092] use Figure 1 The process flow shown is illustrated, and the process parameters involved are listed in Table 3. The distribution and properties of the resulting products are listed in Table 4.

[0093] Table 3

[0094]

[0095] Table 3 (continued)

[0096]

[0097] Table 4

[0098]

[0099]

[0100] From the results of Table 4, it can be seen that the method of the present application for converting refinery low-value naphtha into olefin feed has high selectivity for propane, while also appropriately taking into account the effects of n-butane, C5, and C6.

[0101] In addition, from the results of Example 3 and Example 4 above, it can be seen that using a hydrocracking catalyst within the preferred range for converting the target feedstock can result in similar product distributions, but depending on the performance differences of the catalysts, the reaction conditions required are slightly different.

[0102] The preferred embodiments of the present application have been described in detail above, but the present application is not limited thereto. Various simple modifications can be made to the technical solutions of the present application within the technical concept of the present application, including combining each technical feature in any other suitable manner, and these simple modifications and combinations should also be considered as disclosed by the present application and fall within the protection scope of the present application.

Claims

1. A hydrocracking process for producing an olefin feed from a light oil characterized in that, The method is carried out in a system comprising a hydrogenation cracking reactor I and a hydrogenation cracking reactor II arranged in parallel, and comprises the following steps: (1) introducing raw oil I and raw oil II into the hydrogenation cracking reactor I and the hydrogenation cracking reactor II respectively under low-pressure hydrogen conditions to carry out hydrogenation cracking reactions, to obtain hydrogenation cracking products I and II respectively; (2) separating the hydrogenation cracking products I and II to obtain C3 / C4 products and C5 and above light naphtha products; The raw oil I and the raw oil II are each independently selected from at least one of light oils; the naphthene content in the raw oil I is 40wt%-100wt%, and the total saturated hydrocarbon content is ≮70wt%; the naphthene content in the raw oil II is 0wt%-40wt%, and the total saturated hydrocarbon content is ≮70wt%; The conversion rate I of the raw oil I is 38%-95%, and the conversion rate II of the raw oil II is 42%-96%; The conversion rate I = (1-mass percentage content of C5 and above hydrocarbons in the liquid product of the hydrogenation cracking product of the hydrogenation cracking reactor I * yield of the liquid product of the hydrogenation cracking product of the hydrogenation cracking reactor I / mass percentage content of C5 and above hydrocarbons in the raw oil I) * 100%; and the conversion rate II = (1-mass percentage content of C5 and above hydrocarbons in the liquid product of the hydrogenation cracking product of the hydrogenation cracking reactor II * yield of the liquid product of the hydrogenation cracking product of the hydrogenation cracking reactor II / mass percentage content of C5 and above hydrocarbons in the raw oil II) * 100%. The hydrogenation cracking catalyst I and the hydrogenation cracking catalyst II are different, and the hydrogenation cracking catalyst II contains at least one of a ZSM type molecular sieve and a modified product of the ZSM type molecular sieve as an acid component.

2. The hydrocracking process of claim 1, wherein, The light oil has a carbon number of C5-C12, and a saturated hydrocarbon content of 70wt%-90wt%.

3. The hydrocracking process of claim 1 or 2, wherein, The light oil has a dry point of not higher than 200℃, a paraffin content of 30wt%-100wt%, and an aromatic hydrocarbon content of 0wt%-30wt%.

4. The hydrocracking process of claim 1 or 2, wherein, The raw oil I has a paraffin content of 30wt%-60wt% and a naphthene content of 40wt%-70wt%, and the raw oil II has a paraffin content of ≮80wt% and a naphthene content of ≯20wt%.

5. The hydrocracking process of claim 1 or 2, wherein, The light oil is selected from the group consisting of hydrogenation cracking naphtha, ethylene raffinate, reforming raffinate, and DCC gasoline hydrogenation device raffinate.

6. The hydrocracking process of claim 1 or 2, wherein, The nitrogen content in the light oil is ≯20μg / g.

7. The hydrocracking process of claim 1 or 2, wherein, The conditions of the hydrocracking reaction each independently satisfy: a temperature of 280-420℃, a pressure of 0.2-8.0 MPa, a volume space velocity of 0.1-20.0 h -1 , and a hydrogen / oil volume ratio of 100-2000.

8. The hydrocracking process of claim 1 or 2, wherein, The conditions of the hydrocracking reaction in the hydrocracking reactor I satisfy: the temperature is 330-420℃, the pressure is 1.0-8.0MPa, the volume space velocity is 2.0-16.0h -1 , and the hydrogen / oil volume ratio is 500-2000.

9. The hydrocracking process of claim 1 or 2, wherein, The conditions of the hydrocracking reaction in the hydrocracking reactor II satisfy: temperature is 280~380℃, pressure is 0.1~6.4MPa, volume space velocity is 0.5~16.0h -1 , hydrogen oil volume ratio is 300~1000.

10. The hydrocracking process of claim 1 or 2, wherein, The hydrogenation cracking catalyst I and the hydrogenation cracking catalyst II each contain an active metal component and a carrier, and the carrier contains an acid component; and the content of the active metal component in the hydrogenation cracking catalyst I and the hydrogenation cracking catalyst II is each independently 10wt%-50wt% in terms of oxides.

11. The hydrocracking process of claim 10 wherein, In the hydrocracking catalyst I and the hydrocracking catalyst II, the active metal elements in the active metal component are selected from at least two of a Group VIB metal element and a Group VIII metal element.

12. The hydrocracking process of claim 10, wherein, The active metal elements include at least one selected from a Group VIB metal element and at least one selected from a Group VIII metal element.

13. The hydrocracking process of claim 12 wherein, In the hydrocracking catalyst I and the hydrocracking catalyst II, the content of the Group VIB metal element is independently 5wt%-35wt% and the content of the Group VIII metal element is independently 1wt%-8wt% in terms of oxides, based on the total weight of the hydrocracking catalyst.

14. The hydrocracking process of claim 10, wherein, In the hydrocracking catalyst I and the hydrocracking catalyst II, the content of the acid component is independently 45wt%-80wt% based on the total weight of the carrier.

15. The hydrocracking process of claim 14, wherein, In the hydrocracking catalyst I, the acid component is at least one of a β-type molecular sieve, a modified product of a β-type molecular sieve, a Y-type molecular sieve and a modified product of a Y-type molecular sieve.

16. The hydrocracking process of claim 10, wherein, The carrier further contains a heat-resistant inorganic oxide, and the heat-resistant inorganic oxide is silicon oxide and / or aluminum oxide.

17. The hydrocracking process of claim 16, wherein, The content of the heat-resistant inorganic oxide is 20wt%-55wt% based on the weight of the carrier.

18. The hydrocracking process of claim 1 or 2, wherein, The loading volume of the hydrocracking catalyst I is 30%-70% and the loading volume of the hydrocracking catalyst II is 30%-70% based on the total volume of the catalysts in the hydrocracking reactor I and the hydrocracking reactor II.

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