Method and system for producing chemical raw materials through crude oil hydrocracking

Abstract

The invention relates to a method and a system for producing a chemical raw material by crude oil hydrocracking, petroleum crude oil is firstly directly subjected to fractionation treatment, and then obtained gas phase products, chemical light oil products, middle-section oil fractions and optional heavy fractions are respectively treated, so that investment and energy consumption caused by direct hydrogenation treatment of the petroleum crude oil are avoided; the obtained middle-stage oil fraction is subjected to hydrocracking treatment and then returns to a fractionation unit for fractionation treatment, so that the middle-stage oil fraction can be completely converted into the raw material of the chemical device, and the yield of the raw material of the chemical device can be further improved; in addition, after asphaltene, metal and other impurities are removed from the heavy oil fraction through the heavy oil hydrotreating unit, the heavy oil fraction is mixed with the middle-section oil fraction, and the quality of raw materials of chemical engineering devices can be guaranteed. Besides, by adopting the method disclosed by the invention, devices for atmospheric and vacuum distillation, hydrogenation pretreatment, catalytic reforming and the like in the conventional oil refining process can be omitted, the process flow can be simplified, and the device investment and energy consumption can be reduced.

Description

Technical Field

[0001] The present disclosure relates to the field of petrochemical industry, and in particular, to a method and system for producing chemical raw materials by hydrocracking of crude oil. Background Art

[0002] In recent years, with the overcapacity of oil refining equipment, the demand for liquid fuel oil for transportation has reached a peak, and the proportion of oil used in chemical industry has increased year by year, the focus of oil refining enterprises has gradually shifted from ensuring the demand for refined oil to producing high-end chemical raw materials. The conventional method of processing crude oil into chemical materials requires that the crude oil undergoes pre-hydrogenation reaction, hydrofining reaction and hydrocracking reaction, and the reaction effluent is separated by gas and liquid and then enters the fractionation tower to obtain chemical materials. However, this method has problems such as high energy consumption of the equipment and low yield of chemical raw materials. Summary of the invention

[0003] The purpose of the present invention is to provide a method and system for producing chemical raw materials from crude oil, so as to solve the problems of high system energy consumption and low chemical raw material yield existing in the prior art.

[0004] In order to achieve the above-mentioned object, the first aspect of the present disclosure provides a method for producing chemical raw materials from crude oil, the method comprising: subjecting the petroleum crude oil to fractionation treatment in a fractionation unit to obtain gas products, chemical light oil products, middle oil fractions and optional heavy oil fractions; subjecting the middle oil fractions to hydrocracking treatment in a hydrocracking unit to obtain hydrocracking products; subjecting the hydrocracking products to the fractionation unit to the fractionation treatment;

[0005] Optionally, the heavy oil fraction is subjected to heavy oil hydrogenation treatment in a heavy oil hydrogenation unit, and the obtained heavy oil hydrogenation product is mixed with the mid-stage oil fraction and then enters the hydrocracking unit.

[0006] Optionally, the operating conditions of the crude oil fractionation unit include: the operating conditions of the fractionation unit include: the distillation cut point between the gas product and the chemical light oil product is 40-80°C, preferably 50-65°C; the distillation cut point between the chemical light oil product and the mid-section oil fraction is 160-200°C, preferably 170-185°C; the distillation cut point between the mid-section oil fraction and the heavy oil fraction is 480-550°C, preferably 500-520°C.

[0007] Optionally, the operating conditions of the heavy oil hydrogenation unit include: inlet temperature of 250-420°C, hydrogen partial pressure of 12.0-16.0 MPa, volume space velocity of 0.2-1.5 h -1 , hydrogen oil volume ratio 400~1000Nm 3 / m 3 .

[0008] Optionally, the hydrocracking unit comprises a hydrofining reactor and a hydrocracking reactor arranged in series; the method further comprises subjecting the mid-section oil fraction to the hydrofining reactor and the hydrocracking reactor in sequence for the hydrocracking treatment.

[0009] Optionally, the operating conditions of the hydrocracking unit include: a hydrogen partial pressure of 10.0 to 15.0 MPa, a hydrogen to oil volume ratio of 500 to 1000 Nm 3 / m 3 The inlet temperature of the hydrotreating reactor is 340-380°C, and the volume space velocity of the hydrotreating reactor is 1.0-2.0h -1 The volume space velocity of the hydrocracking reactor is 1.5 to 2.8 h -1 .

[0010] Optionally, the catalyst used in the hydrocracking treatment includes a hydrorefining catalyst and a hydrocracking catalyst; the hydrorefining catalyst includes a carrier and an active metal component loaded on the carrier; the carrier includes aluminum oxide and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W; the hydrocracking catalyst includes a carrier and an active metal component loaded on the carrier, the carrier includes aluminum oxide and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W.

[0011] Optionally, the catalyst used in the heavy oil hydroprocessing includes a heavy oil hydrogenation catalyst; the heavy oil hydrogenation catalyst includes a carrier and an active metal component loaded on the carrier, the carrier includes aluminum oxide and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W.

[0012] Optionally, the API gravity of the petroleum crude oil is 10-50, the asphaltene content is less than 6000 μg / g, and the metal content is less than 150 μg / g.

[0013] Optionally, the method further comprises, before the fractionation treatment, subjecting the petroleum crude oil to a desalting treatment.

[0014] The second aspect of the present disclosure is a system for producing chemical raw materials using the method described in the first aspect, the system comprising a fractionation unit, a hydrocracking unit and an optional heavy oil hydrogenation unit; the fractionation unit comprises a petroleum crude oil inlet, a hydrocracking product inlet, a gas phase product outlet, a chemical light oil product outlet, a mid-section oil fraction outlet and an optional heavy oil fraction outlet; the hydrocracking unit comprises a mid-section oil fraction inlet, a heavy oil hydrogenation product inlet and a hydrocracking product outlet; the heavy oil hydrogenation unit comprises a heavy oil fraction inlet and a heavy oil hydrogenation product outlet; the petroleum crude oil inlet of the fractionation unit is connected to a petroleum crude oil source, the mid-section oil fraction outlet of the fractionation unit is connected to the mid-section oil fraction inlet of the hydrocracking unit; the hydrocracking product outlet of the hydrocracking unit is connected to the hydrocracking product inlet of the fractionation unit;

[0015] Optionally, the heavy oil fraction inlet of the heavy oil hydrogenation unit is connected to the heavy oil fraction outlet of the fractionation unit; the heavy oil hydrogenation product outlet of the heavy oil hydrogenation unit is connected to the heavy oil hydrogenation product inlet of the hydrocracking unit.

[0016] Through the above technical scheme, the crude oil is first directly fractionated, and then the obtained gas phase products, chemical light oil products, middle oil fractions and optional heavy fractions are treated separately, avoiding direct hydrogenation of crude oil to cause investment and energy consumption; the obtained middle oil fraction is returned to the fractionation unit for fractionation after hydrocracking treatment, and the middle oil fraction can be completely converted into chemical plant raw materials, thereby improving the yield of chemical plant raw materials; in addition, the heavy oil fraction is mixed with the middle oil fraction after removing asphaltene, metal and other impurities in the heavy oil hydroprocessing unit, which can ensure the quality of the chemical plant raw materials. In addition, the method disclosed in the present invention can save the atmospheric and vacuum pressure, hydrogenation pretreatment and catalytic reforming devices in the conventional oil refining process, simplify the process flow, and reduce device investment and energy consumption.

[0017] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0019] Figure 1 It is a flow chart of the method for producing chemical raw materials from crude oil in Example 1 of the present disclosure.

[0020] Figure 2 It is a flow chart of the method for producing chemical raw materials from crude oil in Example 2 of the present disclosure.

[0021] Description of Reference Numerals

[0022] 1. Fractionation unit; 2. Heavy oil hydrogenation unit; 3. Hydrocracking unit; 11. Petroleum crude oil; 12. Gas products; 13. Chemical light oil products; 14. Mid-section oil fraction; 15. Heavy oil fraction; 16. Heavy oil hydrogenation products; 17. Hydrocracking products; 18. Mid-section and heavy oil fractions. DETAILED DESCRIPTION

[0023] The specific implementation of the present disclosure is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described herein is only used to illustrate and explain the present disclosure, and is not used to limit the present disclosure.

[0024] The first aspect of the present disclosure provides a method for producing chemical raw materials from crude oil, the method comprising: subjecting the petroleum crude oil to fractionation treatment in a fractionation unit to obtain gas products, chemical light oil products, middle oil fractions and optional heavy oil fractions; subjecting the middle oil fractions to hydrocracking treatment in a hydrocracking unit to obtain hydrocracking products; subjecting the hydrocracking products to fractionation treatment in a fractionation unit;

[0025] Optionally, the heavy oil fraction is subjected to heavy oil hydrogenation treatment in a heavy oil hydrogenation unit, and the obtained heavy oil hydrogenation product is mixed with the mid-stage oil fraction and then enters the hydrocracking unit.

[0026] Through the above technical scheme, the crude oil is first directly fractionated, and then the obtained gas phase products, chemical light oil products, middle oil fractions and optional heavy fractions are treated separately, avoiding direct hydrogenation of crude oil to cause investment and energy consumption; the obtained middle oil fraction is returned to the fractionation unit for fractionation after hydrocracking treatment, and the middle oil fraction can be completely converted into chemical plant raw materials, thereby improving the yield of chemical plant raw materials; in addition, the heavy oil fraction is mixed with the middle oil fraction after removing asphaltene, metal and other impurities in the heavy oil hydroprocessing unit, which can ensure the quality of the chemical plant raw materials. In addition, the method disclosed in the present invention can save the atmospheric and vacuum pressure, hydrogenation pretreatment and catalytic reforming devices in the conventional oil refining process, simplify the process flow, and reduce device investment and energy consumption.

[0027] The petroleum crude oil 11 used in the present disclosure is a crude oil or a mixture of multiple crude oils, wherein the crude oil is conventionally selected in the art, and the present application does not impose any restrictions on the source of the crude oil. In a preferred embodiment, the API gravity of the petroleum crude oil 11 is 10 to 50, the asphaltene content is less than 6000 μg / g, and the metal content is less than 150 μg / g. The metals in the crude oil include metal elements such as Fe, Ca, Ni and V.

[0028] In one embodiment, the method further includes pre-treating the crude oil 11 before fractionation, and the pre-treatment includes dehydration and desalination. Dehydration and desalination are both conventional choices in the art, and the present application does not make special requirements for the processes of dehydration and desalination. For example, desalination can be performed using an electric desalination system to remove inorganic salts in the crude oil 11 to prevent inorganic salts from affecting the quality of the product during subsequent processing.

[0029] In one embodiment, the petroleum crude oil 11 after dehydration and / or desalting is fractionated in the fractionation unit 1 to separate the easily separable gas products 12 and chemical light oil products 13 in the petroleum crude oil 11 from the mid-section oil fraction 14 and the heavy oil fraction 15, and then the mid-section oil fraction 14 and the heavy oil fraction 15 are processed separately. On the one hand, it can solve the problem of increased energy consumption and investment caused by directly processing the petroleum crude oil 11; on the other hand, it can reduce the pressure of subsequent processing units to process a large amount of materials; on the other hand, targeted processing of different materials can improve the corresponding processing effect, and thus can further improve the yield of the target product while ensuring the quality of the raw materials of the chemical plant.

[0030] The device of the fractionation unit 1 can be an atmospheric pressure tower or a vacuum tower, preferably an atmospheric pressure tower.

[0031] Among them, in order to take into account both energy saving and separation effect, the operating conditions of the distillation unit 1 are limited. The specific operating conditions of the distillation unit 1 include: the distillation cutting point between the gas product and the chemical light oil product is 40-80°C, preferably 50-65°C; the distillation cutting point between the chemical light oil product and the middle oil fraction is 160-200°C, preferably 170-185°C; the distillation cutting point between the middle oil fraction and the heavy oil fraction is 480-550°C, preferably 500-520°C.

[0032] In one embodiment, the chemical light oil product 13 that is easily separated from the crude oil 11 mainly includes naphtha components such as C5 / C6, so the chemical light oil product 13 can be directly used as a raw material for a chemical plant and discharged from the system.

[0033] In one embodiment, the heavy oil fraction 15 mainly includes components such as heavy oil fraction with a distillation range of ≮480°C, asphaltene, and metals. The present disclosure allows the heavy oil fraction 15 and hydrogen to enter the heavy oil hydrogenation unit 2 to contact with the heavy oil hydrogenation catalyst for heavy oil hydrogenation treatment, and a heavy oil hydrogenation product 16 can be obtained. In this embodiment, the heavy oil fraction 15 can be hydrogenated to remove asphaltene and metal impurities, and the quality of the raw materials of the chemical plant can be further guaranteed.

[0034] Among them, the reactor of the heavy oil hydrogenation unit 2 is conventionally selected in the art, for example, the reactor can be one or more of a fixed bed reactor, an ebullating bed reactor and a suspended bed reactor; preferably, the reactor of the heavy oil hydrogenation unit 2 is a plurality of fixed bed reactors arranged in series, and a mixed hydrogen inlet is provided between two adjacent fixed bed reactors.

[0035] The heavy oil hydrogenation catalyst comprises a carrier and an active metal component supported on the carrier; the carrier comprises alumina and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W. The content of the active metal component is 5 to 40% by weight based on the total weight of the heavy oil hydrogenation catalyst.

[0036] The operating conditions of the heavy oil hydrogenation unit 2 include: inlet temperature of 250-420°C, preferably 360-420°C; hydrogen partial pressure of 12.0-16.0 MPa, preferably 13-16 MPa; volume space velocity of 0.2-1.5 h -1 , preferably 0.2 to 1.3 h -1 ; Hydrogen oil volume ratio 400~1000Nm 3 / m 3 , preferably 600~1000Nm 3 / m 3 .

[0037] In one embodiment, the hydrocracking unit 3 includes a hydrofining reactor and a hydrocracking reactor connected in series.

[0038] Wherein, the hydrotreating reactor and the hydrocracking reactor are both fixed bed reactors, the hydrotreating reactor comprises 1 to 4 catalyst beds, the hydrocracking reactor comprises 2 to 7 catalyst beds, and a mixed hydrogen inlet is provided between two adjacent catalyst beds.

[0039] The method further comprises: firstly allowing the middle oil fraction 14 and hydrogen to enter a hydrotreating reactor and contact with a hydrotreating catalyst for hydrotreating treatment to obtain a hydrotreating product; and then allowing the hydrotreating product and hydrogen to enter a hydrocracking reactor and contact with a hydrocracking catalyst for hydrocracking treatment to obtain a hydrocracking product 17.

[0040] The middle oil fraction 14 mainly includes components such as diesel and wax oil.

[0041] Wherein, the catalyst used in the hydrocracking treatment includes a hydrorefining catalyst and a hydrocracking catalyst.

[0042] The hydrorefining catalyst comprises a carrier and an active metal component loaded on the carrier; the carrier comprises aluminum oxide and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W; based on the total weight of the hydrorefining catalyst, the content of the active metal component is 5 to 40 weight %.

[0043] The hydrocracking catalyst comprises a carrier and an active metal component supported on the carrier. The carrier comprises aluminum oxide and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W. The content of the active metal component is 5 to 40% by weight based on the total weight of the hydrocracking catalyst.

[0044] The operating conditions of the hydrocracking unit 3 include: a hydrogen partial pressure of 10.0 to 15.0 MPa, preferably 12 to 15 MPa; a hydrogen to oil volume ratio of 500 to 1000 Nm 3 / m 3 , preferably 600~1000Nm 3 / m 3 The inlet temperature of the hydrotreating reactor is 340-380°C, preferably 340-365°C; the volume space velocity of the hydrotreating reactor is 1.0-2.0h -1 , preferably 1.1 to 1.9 hours -1 The volume space velocity of the hydrocracking reactor is 1.5 to 2.8 h -1 , preferably 1.8 to 2.6 hours -1 .

[0045] In one embodiment, when the crude oil is light crude oil or the metal and asphaltene content in the crude oil is low, the heavy oil hydrogenation unit 2 can be eliminated, and the petroleum crude oil 11 is separated by the distillation unit 1 to obtain gas products 12, chemical light oil products 13, and middle and heavy oil fractions, and the middle and heavy oil fractions are all sent to the hydrocracking unit 3 for hydrocracking treatment.

[0046] In one embodiment, a light hydrocarbon recovery, naphtha stabilization, and normal isobutane separation system can be set up according to demand, and the gas product 12 in the entire system can be centrally separated and recovered to produce high-quality liquefied gas products and stabilized naphtha. Furthermore, the liquefied gas can be separated into propane, normal butane, and isobutane components according to demand.

[0047] In one embodiment, if Figure 1 As shown, the method for producing chemical raw materials by hydrocracking of crude oil includes:

[0048] The petroleum crude oil 11 is subjected to fractionation treatment in a fractionation unit 1 to obtain a gas product 12, a chemical light oil product 13, a middle oil fraction 14 and a heavy oil fraction 15; the operating conditions of the fractionation unit 1 include: the fraction cut point between the gas product and the chemical light oil product is 40-80°C; the fraction cut point between the chemical light oil product and the middle oil fraction is 160-200°C; the fraction cut point between the middle oil fraction and the heavy oil fraction is 480-550°C;

[0049] The middle oil fraction 14 and hydrogen are firstly introduced into a hydrofining reactor to contact with a hydrofining catalyst for hydrofining treatment to obtain a hydrofining product; the hydrofining product and hydrogen are introduced into a hydrocracking reactor to contact with a hydrocracking catalyst for hydrocracking treatment to obtain a hydrocracking product 17; the hydrocracking product 17 is returned to the fractionation unit 1 for further separation. The operating conditions of the hydrocracking unit 3 include: a hydrogen partial pressure of 10.0 to 15.0 MPa, a hydrogen-to-oil volume ratio of 500 to 1000 Nm 3 / m 3 The inlet temperature of the hydrotreating reactor is 340-380°C, and the volume space velocity of the hydrotreating reactor is 1.0-2.0h -1 The volume space velocity of the hydrocracking reactor is 1.5 to 2.8 h -1 ;

[0050] The heavy oil fraction 15 and hydrogen enter the heavy oil hydrogenation unit 2 to contact with the heavy oil hydrogenation catalyst for heavy oil hydrogenation treatment, and the obtained heavy oil hydrogenation product 16 is mixed with the middle oil fraction 14 and then enters the hydrocracking unit 3; the operating conditions of the heavy oil hydrogenation unit 2 include: inlet temperature of 250-420°C, hydrogen partial pressure of 12.0-16.0MPa, volume space velocity of 0.2-1.0h -1 , hydrogen oil volume ratio 400~1000Nm 3 / m 3 .

[0051] The second aspect of the present disclosure is a system for producing chemical raw materials using the method described in the first aspect, the system comprising a fractionation unit 1, a hydrocracking unit 3 and an optional heavy oil hydrogenation unit 2; the fractionation unit 1 comprises a petroleum crude oil inlet, a hydrocracking product inlet, a gas phase product outlet, a chemical light oil product outlet, a mid-section oil fraction outlet and an optional heavy oil fraction outlet; the hydrocracking unit 3 comprises a mid-section oil fraction inlet, a heavy oil hydrogenation product inlet and a hydrocracking product outlet; the heavy oil hydrogenation unit 2 comprises a heavy oil fraction inlet and a heavy oil hydrogenation product outlet;

[0052] The crude oil inlet of the fractionation unit 1 is connected to the crude oil source, so that the crude oil can be fractionated; the middle oil fraction outlet of the fractionation unit 1 is connected to the middle oil fraction inlet of the hydrocracking unit 3, so that the middle oil fraction can be hydrocracking; the hydrocracking product outlet of the hydrocracking unit 3 is connected to the hydrocracking product inlet of the fractionation unit 1, so that the hydrocracking product can be returned to the fractionation unit 1 for fractionation;

[0053] Optionally, the heavy oil fraction inlet of the heavy oil hydrogenation unit 2 is connected to the heavy oil fraction outlet of the fractionation unit 1, so that the heavy oil fraction 15 can enter the heavy oil hydrogenation unit 2 for heavy oil hydrogenation treatment; the heavy oil hydrogenation product outlet of the heavy oil hydrogenation unit 2 is connected to the heavy oil hydrogenation product inlet of the hydrocracking unit 3, so that the heavy oil hydrogenation product 16 can enter the hydrocracking unit 3 to participate in the hydrocracking treatment.

[0054] The present disclosure is further described in detail by way of examples. The raw materials used in the examples can all be obtained through commercial sources. The properties of the petroleum crude oil used in the following examples and comparative examples are shown in Table 1, wherein the composition and content of the heavy oil hydrogenation catalyst, the hydrorefining catalyst and the hydrocracking catalyst are shown in Table 2.

[0055] Table 1 Properties of crude oil

[0056]

[0057]

[0058] Table 2 Composition and content of catalyst

[0059]

[0060] Example 1

[0061] Systems for producing chemical raw materials from crude oil, such as Figure 1 As shown, the method for producing chemical raw materials by hydrocracking of crude oil includes:

[0062] A petroleum crude oil 11 (crude oil A) is subjected to fractionation treatment in a fractionation unit 1 to obtain a gas product 12, a chemical light oil product 13, a middle oil fraction 14 and a heavy oil fraction 15; the operating conditions of the fractionation unit 1 include: a fraction cut point between the gas product and the chemical light oil product is 50° C.; a fraction cut point between the chemical light oil product and the middle oil fraction is 175° C.; a fraction cut point between the middle oil fraction and the heavy oil fraction is 520° C.;

[0063] The middle oil fraction 14 and hydrogen are firstly introduced into a hydrofining reactor to contact with a hydrofining catalyst for hydrofining treatment to obtain a hydrofining product; the hydrofining product and hydrogen are introduced into a hydrocracking reactor to contact with a hydrocracking catalyst for hydrocracking treatment to obtain a hydrocracking product 17; the hydrocracking product 17 is returned to the fractionation unit 1 for further separation. The operating conditions of the hydrocracking unit 3 include: a hydrogen partial pressure of 15 MPa, a hydrogen-to-oil volume ratio of 750 Nm 3 / m 3 The inlet temperature of the hydrotreating reactor is 355°C, and the volume space velocity of the hydrotreating reactor is 1.3h -1 The volume space velocity of the hydrocracking reactor is 1.8h -1 ;

[0064] The heavy oil fraction 15 and hydrogen enter the heavy oil hydrogenation unit 2 to contact with the heavy oil hydrogenation catalyst for heavy oil hydrogenation treatment, and the obtained heavy oil hydrogenation product 16 is mixed with the middle oil fraction 14 and then enters the hydrocracking unit 3; the operating conditions of the heavy oil hydrogenation unit 2 include: inlet temperature of 362°C, hydrogen partial pressure of 15.5MPa, volume space velocity of 1.3h -1 , hydrogen oil volume ratio 800Nm 3 / m 3 .

[0065] The properties of the products are shown in Table 3.

[0066] Example 2

[0067] Systems for producing chemical raw materials from crude oil, such as Figure 2 As shown;

[0068] The method for producing chemical raw materials from crude oil is the same as that in Example 1, except that petroleum crude oil 11 (crude oil B) is fractionated in a fractionation unit 1 to obtain a gas product 12, a chemical light oil product 13, and a middle and heavy oil fraction 18; the middle and heavy oil fraction 18 are all fed into a hydrocracking unit 3, wherein the fraction cut point of the chemical light oil product 13 and the middle and heavy oil fraction 18 is 175°C.

[0069] Comparative Example 1

[0070] The petroleum crude oil in Example 1 was mixed with hydrogen and then passed through a pretreatment reaction zone, a hydrotreating reaction zone and a hydrocracking reaction zone in sequence, and was contacted with a hydrogenation protective agent, a hydrodemetallization agent, a hydrotreating catalyst, a hydrocracking catalyst and a post-hydrotreating catalyst in sequence for reaction. The properties of the obtained product are shown in Table 3.

[0071] Comparative Example 2

[0072] Crude oil B was used as the petroleum crude oil and was processed by the method in Comparative Example 1. The properties obtained are shown in Table 3.

[0073] Table 3 Products of Examples and Comparative Examples

[0074]

[0075]

[0076] As shown in Table 3, according to the comparison of the data of Example 1 and Comparative Example 1, and Example 2 and Comparative Example 2, it can be seen that the method disclosed in the present invention can not only ensure the quality of the raw materials of the chemical plant, but also improve the yield of the raw materials of the chemical plant, and can also reduce energy consumption and investment.

[0077] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings; however, the present disclosure is not limited to the specific details in the above embodiments. Within the technical concept of the present disclosure, a variety of simple modifications can be made to the technical solution of the present disclosure, and these simple modifications all fall within the protection scope of the present disclosure.

[0078] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present disclosure will not further describe various possible combinations.

[0079] In addition, various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A method for producing chemical raw materials from crude oil, characterized in that: The method includes: The crude oil is subjected to fractionation treatment in a fractionation unit (1) to obtain a gas product, a chemical light oil product, a mid-range oil fraction and an optional heavy oil fraction; The middle oil fraction is fed into a hydrocracking unit (3) for hydrocracking treatment to obtain a hydrocracking product; Allowing the hydrocracking product to enter the fractionation unit (1) for the fractionation treatment; Optionally, the heavy oil fraction is subjected to heavy oil hydrogenation treatment in a heavy oil hydrogenation unit (2), and the obtained heavy oil hydrogenation product is mixed with the mid-stage oil fraction and then enters the hydrocracking unit (3).

2. The method according to claim 1, characterized in that The operating conditions of the fractionation unit (1) include: the cut point between the gas product and the chemical light oil product is 40-80°C, preferably 50-65°C; the cut point between the chemical light oil product and the mid-section oil fraction is 160-200°C, preferably 170-185°C; the cut point between the mid-section oil fraction and the heavy oil fraction is 480-550°C, preferably 500-520°C.

3. The method according to claim 1, characterized in that The operating conditions of the heavy oil hydrogenation unit (2) include: an inlet temperature of 250-420°C, a hydrogen partial pressure of 12.0-16.0 MPa, and a volume space velocity of 0.2-1.5 h -1 , hydrogen oil volume ratio 400~1000Nm 3 / m 3 .

4. The method according to claim 1, characterized in that: The hydrocracking unit (3) comprises a hydrofining reactor and a hydrocracking reactor arranged in series; The method further comprises subjecting the middle oil fraction to the hydrotreating reactor and the hydrocracking reactor in sequence for the hydrocracking treatment.

5. The method according to claim 4, characterized in that The operating conditions of the hydrocracking unit (3) include: a hydrogen partial pressure of 10.0 to 15.0 MPa, a hydrogen to oil volume ratio of 500 to 1000 Nm 3 / m 3 The inlet temperature of the hydrotreating reactor is 340-380°C, and the volume space velocity of the hydrotreating reactor is 1.0-2.0h -1 The volume space velocity of the hydrocracking reactor is 1.5 to 2.8 h -1 .

6. The method according to claim 1, characterized in that The catalyst used in the hydrocracking treatment includes a hydrorefining catalyst and a hydrocracking catalyst; The hydrotreating catalyst comprises a carrier and an active metal component supported on the carrier; the carrier comprises alumina and / or silicon oxide, and the active metal component is selected from one or more of Ni, Co, Mo and W; The hydrocracking catalyst comprises a carrier and an active metal component supported on the carrier. The carrier comprises aluminum oxide and / or silicon oxide. The active metal component is selected from one or more of Ni, Co, Mo and W.

7. The method according to claim 1, characterized in that The catalyst used in the heavy oil hydroprocessing includes a heavy oil hydrogenation catalyst; The heavy oil hydrogenation catalyst comprises a carrier and an active metal component supported on the carrier. The carrier comprises aluminum oxide and / or silicon oxide. The active metal component is selected from one or more of Ni, Co, Mo and W.

8. The method according to claim 1, characterized in that The API gravity of the petroleum crude oil is 10-50, the asphaltene content is less than 6000 μg / g, and the metal content is less than 150 μg / g.

9. The method according to claim 1, characterized in that: The method also includes subjecting the petroleum crude oil to desalting treatment prior to the fractionation treatment.

10. A system for producing chemical raw materials using the method according to any one of claims 1 to 9, characterized in that: The system comprises a fractionation unit (1), a hydrocracking unit (3) and an optional heavy oil hydrogenation unit (2); the fractionation unit (1) comprises a crude oil inlet, a hydrocracking product inlet, a gas phase product outlet, a chemical light oil product outlet, a mid-section oil fraction outlet and an optional heavy oil fraction outlet; the hydrocracking unit (3) comprises a mid-section oil fraction inlet, a heavy oil hydrogenation product inlet and a hydrocracking product outlet; the heavy oil hydrogenation unit (2) comprises a heavy oil fraction inlet and a heavy oil hydrogenation product outlet; The petroleum crude oil inlet of the fractionation unit (1) is connected to the petroleum crude oil source, the middle oil fraction outlet of the fractionation unit (1) is connected to the middle oil fraction inlet of the hydrocracking unit (3); the hydrocracking product outlet of the hydrocracking unit (3) is connected to the hydrocracking product inlet of the fractionation unit (1); Optionally, the heavy oil fraction inlet of the heavy oil hydrogenation unit (2) is connected to the heavy oil fraction outlet of the fractionation unit (1); the heavy oil hydrogenation product outlet of the heavy oil hydrogenation unit (2) is connected to the heavy oil hydrogenation product inlet of the hydrocracking unit (3).

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