Method and system for producing chemical material from crude oil

Abstract

The invention relates to a method and system for producing a chemical material from crude oil, and the method comprises the following steps: firstly, carrying out simple pre-fractionation on petroleum crude oil to obtain a light oil fraction and a heavy oil fraction; and then the heavy oil fraction is subjected to impurity removal through the hydrofining unit and enters the product fractionation unit to be divided into a gas product, a chemical light oil product and unconverted oil, and the unconverted oil enters the hydrocracking unit to be subjected to cracking reaction and then is mixed with the heavy fraction oil to be returned to the hydrofining unit. By adopting the method disclosed by the invention, investment and energy consumption caused by direct hydrotreating of the petroleum crude oil can be avoided; and moreover, the yield of raw materials of the chemical device can be improved. 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 materials from crude oil. Background Art

[0002] Generally, crude oil is the oil extracted from underground without being processed. Crude oil can be divided into three categories according to its composition: paraffin-based crude oil, cycloalkyl crude oil and intermediate-based crude oil; according to its sulfur content, it can be divided into four categories: ultra-low sulfur crude oil, low sulfur crude oil, sulfur-containing crude oil and high sulfur crude oil; according to its specific gravity, it can be divided into three categories: light crude oil, medium crude oil and heavy crude oil. In recent years, with the overcapacity of oil refining units, the demand for liquid fuel oil for transportation has reached a peak. Therefore, the focus of oil refining companies 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 undergo pre-hydrogenation reaction, hydrofining reaction and hydrocracking reaction to obtain the reaction effluent, which enters the distillation tower after gas-liquid separation 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 materials from crude oil, so as to solve the problems of high energy consumption and low yield of chemical raw materials in the prior art.

[0004] In order to achieve the above-mentioned purpose, the first aspect of the present disclosure provides a method for producing chemical materials from crude oil, which method comprises: subjecting the petroleum crude oil to a first fractionation treatment in a crude oil fractionation unit to obtain a light oil fraction and a heavy oil fraction; subjecting the heavy oil fraction to a hydrorefining unit for a hydrorefining treatment to obtain a hydrorefining product; subjecting the hydrorefining product to a second fractionation treatment in a product fractionation unit to obtain a gas product, a chemical light oil product and an unconverted oil; subjecting the unconverted oil to a hydrocracking unit for a hydrocracking treatment, and mixing the obtained hydrocracking product with the heavy oil fraction and returning it to the hydrorefining unit.

[0005] Optionally, the operating conditions of the crude oil fractionation unit include: the cut point of the light oil fraction and the heavy oil fraction is 160-200°C, preferably 170-185°C; the operating conditions of the product fractionation unit include: the cut point of the gas product and the chemical light oil product is 40-80°C, preferably 50-65°C; the cut point of the chemical light oil product and the unconverted oil is 160-200°C, preferably 170-185°C.

[0006] Optionally, the reactor in the hydrotreating unit is selected from one or more of a fixed bed reactor, an ebullating bed reactor and a suspended bed reactor; the operating conditions of the hydrotreating unit include: an inlet temperature of 250 to 420°C, a hydrogen partial pressure of 8.0 to 14.5 MPa, a volume space velocity of 1.0 to 2.0 h-1 , hydrogen oil volume ratio 500~1000Nm 3 / m 3 .

[0007] Optionally, the operating conditions of the hydrocracking unit include: inlet temperature of 340-380°C, hydrogen partial pressure of 10.0-15.0 MPa, volume space velocity of 1.5-2.8 h -1 , hydrogen to oil volume ratio is 500~1000Nm 3 / m 3 .

[0008] Optionally, the API gravity of the petroleum crude oil is ≮10, the asphaltene content is less than 6000 μg / g, and the metal content is less than 150 μg / g.

[0009] Optionally, the reactor in the hydrocracking unit is a fixed bed reactor or an ebullated bed reactor; when the API of the petroleum crude oil is ≮26, the reactor in the hydrocracking unit is a fixed bed reactor; when the API of the petroleum crude oil is 10-26, the reactor in the hydrocracking unit is an ebullated bed reactor.

[0010] Optionally, the catalyst used in the hydrotreating treatment includes a hydrotreating catalyst; the hydrotreating 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 hydrocracking treatment includes a hydrocracking catalyst; the hydrocracking catalyst includes a carrier and an active metal component supported on the carrier, wherein 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 crude oil fractionation unit is an atmospheric pressure fractionation tower or a vacuum fractionation tower, preferably an atmospheric pressure fractionation tower; the product fractionation unit is an atmospheric pressure fractionation tower or a vacuum fractionation tower, preferably an atmospheric pressure fractionation tower.

[0013] The second aspect of the present disclosure is a system for producing chemical materials using the method described in the first aspect, the system comprising a crude oil fractionation unit, a hydrorefining unit, a product fractionation unit and a hydrocracking unit; the crude oil fractionation unit comprises a petroleum crude oil inlet, a light oil fraction outlet and a heavy oil fraction outlet; the hydrorefining unit comprises a heavy oil fraction inlet, a hydrocracking product inlet and a hydrorefining product outlet; the product fractionation unit comprises a hydrorefining product inlet, a gas product outlet, a chemical light oil product outlet and an unconverted oil outlet; the hydrocracking unit comprises an unconverted The crude oil inlet of the crude oil fractionation unit is connected to the crude oil source, and the heavy oil fraction outlet of the crude oil fractionation unit is connected to the heavy oil fraction inlet of the hydrorefining unit; the hydrorefining product outlet of the hydrorefining unit is connected to the hydrorefining product inlet of the product fractionation unit; the unconverted oil outlet of the product fractionation unit is connected to the unconverted oil inlet of the hydrocracking unit; the hydrocracking product outlet of the hydrocracking unit is connected to the hydrocracking product inlet of the hydrorefining unit.

[0014] Through the above technical scheme, the crude oil is first subjected to simple pre-fractionation to obtain light oil fraction and heavy oil fraction; then the heavy oil fraction is subjected to the hydrofining unit to remove impurities, and enters the product fractionation unit to be divided into gas products, chemical light oil products and unconverted oil. After the unconverted oil enters the hydrocracking unit for cracking reaction, it is mixed with the heavy fraction oil and enters the hydrofining unit; this method directly fractionates the crude oil to avoid directly hydrotreating the crude oil and causing investment and energy consumption; and the light oil fraction, gas phase product and chemical light oil product obtained by pre-fractionation can be directly used as raw materials for chemical plants, which can improve the yield of raw materials for chemical plants; at the same time, the unconverted oil is recycled after being treated, which can improve the utilization rate of the heavy oil fraction and further improve the yield of raw materials for chemical plants. 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.

[0015] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] 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:

[0017] Figure 1 The present invention discloses a flow chart of a method for producing chemical materials from crude oil.

[0018] Description of Reference Numerals

[0019] 1. Crude oil fractionation unit; 2. Hydrofining unit; 3. Product fractionation unit; 4. Hydrocracking unit; 11. Petroleum crude oil; 12. Light oil fraction; 13. Heavy oil fraction; 14. Hydrofining products; 15. Gas products; 16. Chemical light oil products; 17. Unconverted oil; 18. Hydrocracking products. DETAILED DESCRIPTION

[0020] 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.

[0021] In the present disclosure, the terms "first, second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Thus, a feature defined as "first, second" may explicitly or implicitly include one or more of the feature. In the description of the present disclosure, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0022] The first aspect of the present disclosure provides a method for producing chemical raw materials by hydrocracking of crude oil, the method comprising: subjecting petroleum crude oil 11 to a first fractionation treatment in a crude oil fractionation unit 1 to obtain a light oil fraction 12 and a heavy oil fraction 13; subjecting the heavy oil fraction 13 to a hydrorefining unit 2 for hydrorefining treatment to obtain a hydrorefining product 14; subjecting the hydrorefining product 14 to a second fractionation treatment in a product fractionation unit 3 to obtain a gas product 15, a chemical light oil product 16 and an unconverted oil 17; subjecting the unconverted oil 17 to a hydrocracking treatment in a hydrocracking unit 4, and mixing the obtained hydrocracking product 18 with the heavy oil fraction 13 and returning the mixed product to the hydrorefining unit 2.

[0023] Through the above technical scheme, the crude oil 11 is first subjected to simple pre-fractionation to obtain a light oil fraction 12 and a heavy oil fraction 13; then the heavy oil fraction 13 is subjected to a hydrotreating unit 2 to remove impurities, and enters a product fractionation unit 3 to be divided into a gas product 15, a chemical light oil product 16 and an unconverted oil 17; the unconverted oil 17 enters a hydrocracking unit 4 for cracking reaction, and is mixed with the heavy fraction oil and enters the hydrotreating unit 2; the method directly fractionates the crude oil 11 to avoid directly subjecting the crude oil 11 to hydrotreating, which causes investment and energy consumption; and the light oil fraction 12, the gas product 15 and the chemical light oil product 16 obtained by the pre-fractionation can be directly used as raw materials for chemical plants, which can improve the yield of raw materials for chemical plants; at the same time, the unconverted oil 17 can be recycled after being treated, which can improve the utilization rate of the heavy oil fraction 13 and further improve the yield of raw materials for chemical plants. In addition, the method disclosed in the present invention can eliminate the need for atmospheric and vacuum decompression, hydrogenation pretreatment, and catalytic reforming devices in conventional oil refining processes, thereby simplifying the process flow and reducing device investment and energy consumption.

[0024] 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, 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.

[0025] In one embodiment, the method further includes, before the first fractionation treatment, pre-treating the crude oil 11, the pre-treating including 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, so as to prevent the inorganic salts from affecting the quality of the product during the subsequent treatment process.

[0026] In one embodiment, the petroleum crude oil 11 after dehydration and / or desalting is preliminarily fractionated in the crude oil fractionation unit 1 to separate the easily separable light oil fraction 12 and heavy oil fraction 13 in the petroleum crude oil 11, and then the light oil fraction 12 and the heavy oil fraction 13 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, thereby ensuring the quality of the raw materials of the chemical plant while further improving the yield of the target product.

[0027] The crude oil fractionation unit 1 may be a normal pressure fractionation tower or a vacuum fractionation tower, preferably a normal pressure fractionation tower.

[0028] In order to take into account both energy saving and separation effect, the operating conditions of the crude oil fractionation unit 1 are limited. Specifically, the operating conditions of the crude oil fractionation unit 1 include: the fraction cut point between the light oil fraction 12 and the heavy oil fraction 13 is 160-200°C, preferably 170-185°C.

[0029] In one embodiment, the easily separated light oil fraction 12 in the crude oil 11 mainly includes naphtha components such as C5 / C6, so the light oil fraction 12 can be directly used as a raw material for a chemical plant and discharged from the system.

[0030] In one embodiment, the heavy oil fraction 13 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 13 and hydrogen to enter the hydrorefining unit 2 and contact with the hydrorefining catalyst for hydrorefining treatment, and a hydrorefining product 14 can be obtained. In this embodiment, the heavy oil fraction 13 is subjected to hydrorefining treatment. On the one hand, asphaltene and metal impurities can be removed, and on the other hand, the heavy oil fraction 13 can be converted into a chemical light oil product 16. Therefore, the hydrorefining treatment of the present disclosure can ensure the quality of the raw materials of the chemical plant.

[0031] The reactor of the hydrotreating unit 2 is conventionally selected in the art, for example, the reactor may be one or more of a fixed bed reactor, an ebullating bed reactor and a suspended bed reactor.

[0032] The reactor of the hydrotreating unit 2 is preferably a single fixed bed reactor, which includes 2 to 5 catalyst beds, and a mixed hydrogen inlet is provided between two adjacent catalyst beds.

[0033] The catalyst used in the hydrofining treatment includes a hydrofining catalyst; the hydrofining catalyst includes a carrier and an active metal component supported 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. Based on the total weight of the heavy oil hydrogenation catalyst, the content of the active metal component is 5 to 40% by weight.

[0034] The operating conditions of the hydrotreating unit 2 include: inlet temperature of 250-420°C, preferably 360-420°C; hydrogen partial pressure of 8.0-14.5 MPa, preferably 8.5-14 MPa; volume space velocity of 1.0-2.0 h -1 , preferably 1.2 to 1.7 hours -1 ; Hydrogen oil volume ratio 500~1000Nm 3 / m3 , preferably 600~900Nm 3 / m 3 .

[0035] In one embodiment, the device of the product fractionation unit 3 can be an atmospheric pressure fractionation tower or a vacuum fractionation tower, preferably an atmospheric pressure fractionation tower.

[0036] Among them, in order to take into account both energy saving and separation effect, the operating conditions of the product fractionation unit 3 are limited. The specific operating conditions of the product fractionation unit 3 include: the distillation cut point of the gas product 15 and the chemical light oil product 16 is 40-80°C, preferably 50-65°C; the distillation cut point of the chemical light oil product 16 and the unconverted oil 17 is 160-200°C, preferably 170-185°C.

[0037] In one embodiment, the unconverted oil 17 and hydrogen are introduced into the hydrocracking unit 4 to contact with the hydrocracking catalyst for hydrocracking treatment to obtain a hydrocracking product 18; the hydrocracking product 18 is mixed with the heavy oil fraction 13 and returned to the hydrotreating unit 2.

[0038] Among them, the reactor in the hydrocracking unit 4 can be a fixed bed reactor or an ebullating bed reactor; in order to further improve the reaction effect of the hydrocracking reaction, it is necessary to select the type of reactor according to the properties of the petroleum crude oil 11; when the API of the petroleum crude oil 11 is ≮26, the reactor in the hydrocracking unit 4 is a fixed bed reactor; when the API of the petroleum crude oil 11 is 10-26, the reactor in the hydrocracking unit 4 is an ebullating bed reactor.

[0039] The reactor in the hydrocracking unit 4 is preferably a single fixed bed reactor, which includes 2 to 7 catalyst beds, and a mixed hydrogen inlet is provided between two adjacent catalyst beds.

[0040] The operating conditions of the hydrocracking unit 4 include: an inlet temperature of 340-380°C, preferably 340-365°C; a hydrogen partial pressure of 10.0-15.0 MPa, preferably 12-15 MPa; a volume space velocity of 1.5-2.8 h -1 , preferably 1.8 to 2.6 hours -1 ; Hydrogen oil volume ratio is 500~1000Nm 3 / m 3 , preferably 600~1000Nm 3 / m 3 .

[0041] The catalyst used in the hydrocracking treatment includes a hydrocracking catalyst; the hydrocracking catalyst includes a carrier and an active metal component supported 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 content of the active metal component is 5 to 40% by weight based on the total weight of the second hydrocracking catalyst.

[0042] In one embodiment, a light hydrocarbon recovery, naphtha stabilization, and normal isomerized butane separation system can be set up according to demand, and the gas product 15 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.

[0043] In one embodiment, a heating device may be provided on the feed pipeline of the hydrocracking unit 4 to heat the unconverted oil 17 to a temperature required for the hydrocracking reaction. The heating device is conventionally selected in the art, for example, the heating device may be a heating furnace or a heat exchanger.

[0044] In one embodiment, if Figure 1 As shown, the method for producing chemical materials from crude oil includes:

[0045] The petroleum crude oil 11 is subjected to a first fractionation treatment by a crude oil fractionation unit 1 to obtain a light oil fraction 12 and a heavy oil fraction 13; the operating conditions of the crude oil fractionation unit 1 include: the fraction cut point of the light oil fraction 12 and the heavy oil fraction 13 is 160-200°C;

[0046] The heavy oil fraction 13 and hydrogen enter the hydrofining unit 2 to contact with the hydrofining catalyst for hydrofining treatment to obtain a hydrofining product 14; the operating conditions of the hydrofining unit 2 include: an inlet temperature of 250 to 420°C, a hydrogen partial pressure of 8.0 to 14.5 MPa, and a volume space velocity of 1.0 to 2.0 h -1 , hydrogen oil volume ratio 500~1000Nm 3 / m 3 ;

[0047] The hydrofining product 14 is subjected to a second fractionation treatment in a product fractionation unit 3 to obtain a gas product 15, a chemical light oil product 16 and an unconverted oil 17; the operating conditions of the product fractionation unit 3 include: the fraction cut point of the gas product 15 and the chemical light oil product 16 is 40-80° C.; the fraction cut point of the chemical light oil product 16 and the unconverted oil 17 is 160-200° C.;

[0048] The unconverted oil 17 and hydrogen are contacted with a hydrocracking catalyst in a hydrocracking unit 4 for hydrocracking treatment, and the obtained hydrocracking product 18 is mixed with the heavy oil fraction 13 and then returned to the hydrofining unit 2; the operating conditions of the hydrocracking unit 4 include: an inlet temperature of 340 to 380°C, a hydrogen partial pressure of 10.0 to 15.0 MPa, and a volume space velocity of 1.5 to 2.8 h -1 , hydrogen to oil volume ratio is 500~1000Nm 3 / m 3 .

[0049] In a second aspect of the present disclosure, a system for producing chemical materials using the method described in the first aspect is provided, the system comprising a crude oil fractionation unit 1, a hydrorefining unit 2, a product fractionation unit 3 and a hydrocracking unit 4; the crude oil fractionation unit 1 comprises a petroleum crude oil inlet, a light oil fraction outlet and a heavy oil fraction outlet; the hydrorefining unit 2 comprises a heavy oil fraction inlet, a hydrocracking product inlet and a hydrorefining product outlet; the product fractionation unit 3 comprises a hydrorefining product inlet, a gas product outlet, a chemical light oil product outlet and an unconverted oil outlet; the hydrocracking unit 4 comprises an unconverted oil inlet and a hydrocracking product outlet; the petroleum crude oil inlet of the crude oil fractionation unit 1 is connected to a petroleum crude oil source so that the petroleum crude oil 11 enters the crude oil fractionation unit 1 for the first A fractionation treatment; the heavy oil fraction outlet of the crude oil fractionation unit 1 is connected to the heavy oil fraction inlet of the hydrotreating unit 2, so that the heavy oil fraction 13 can be hydrotreating treated; the hydrotreating product outlet of the hydrotreating unit 2 is connected to the hydrotreating product inlet of the product fractionation unit 3, so that the hydrotreating product 14 can be subjected to a second fractionation; the unconverted oil outlet of the product fractionation unit 3 is connected to the unconverted oil inlet of the hydrocracking unit 4, so that the unconverted oil 17 can enter the hydrocracking unit 4 for hydrocracking treatment; the hydrocracking product outlet of the hydrocracking unit 4 is connected to the hydrocracking product inlet of the hydrotreating unit 2, so that the hydrocracking product 18 can return to the hydrotreating unit 2.

[0050] The present disclosure is further described in detail by way of examples. The raw materials used in the examples can 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 hydrorefining catalyst and the hydrocracking catalyst are shown in Table 2.

[0051] Table 1 Properties of crude oil

[0052]

[0053]

[0054] Table 2 Composition and content of catalyst

[0055]

[0056] Example 1

[0057] Systems for producing chemical materials from crude oil Figure 1 As shown, the method for producing chemical materials from crude oil includes:

[0058] The petroleum crude oil 11 is subjected to a first fractionation treatment by a crude oil fractionation unit 1 to obtain a light oil fraction 12 and a heavy oil fraction 13; the operating conditions of the crude oil fractionation unit 1 include: the fraction cut point of the light oil fraction 12 and the heavy oil fraction 13 is 175°C;

[0059] The heavy oil fraction 13 and hydrogen enter the hydrofining unit 2 to contact with the hydrofining catalyst for hydrofining treatment to obtain a hydrofining product 14; the operating conditions of the hydrofining unit 2 include: an inlet temperature of 355°C, a hydrogen partial pressure of 14.5MPa, and a volume space velocity of 1.8h -1 , hydrogen oil volume ratio 750Nm 3 / m 3 ;

[0060] The hydrofining product 14 is subjected to a second fractionation treatment in a product fractionation unit 3 to obtain a gas product 15, a chemical light oil product 16 and an unconverted oil 17; the operating conditions of the product fractionation unit 3 include: the fraction cut point of the gas product 15 and the chemical light oil product 16 is 50° C.; the fraction cut point of the chemical light oil product 16 and the unconverted oil 17 is 175° C.;

[0061] The unconverted oil 17 and hydrogen are contacted with a hydrocracking catalyst in a hydrocracking unit 4 for hydrocracking treatment, and the obtained hydrocracking product 18 is mixed with the heavy oil fraction 13 and then returned to the hydrofining unit 2; the operating conditions of the hydrocracking unit 4 include: an inlet temperature of 358°C, a hydrogen partial pressure of 14 MPa, a volume space velocity of 2.0 h -1 , hydrogen to oil volume ratio is 800Nm 3 / m 3 .

[0062] The properties of the products are shown in Table 3.

[0063] Comparative Example 1

[0064] 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.

[0065] Table 3 Products of Examples and Comparative Examples

[0066]

[0067]

[0068] As shown in Table 3, by comparing the data of Example 1 and Comparative Example 1, it can be seen that the method of the present invention can improve the yield of the raw materials of the chemical plant while ensuring the quality of the raw materials produced; in addition, the method of the present invention can reduce the energy consumption and investment of the device.

[0069] 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, the technical solution of the present disclosure can be subjected to a variety of simple modifications, and these simple modifications all belong to the protection scope of the present disclosure. 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.

[0070] 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 materials from crude oil, characterized in that: The method includes: The petroleum crude oil is subjected to a first fractionation treatment in a crude oil fractionation unit (1) to obtain a light oil fraction and a heavy oil fraction; The heavy oil fraction is fed into a hydrotreating unit (2) for hydrotreating treatment to obtain a hydrotreating product; The hydrofining product is subjected to a second fractionation treatment in a product fractionation unit (3) to obtain a gas product, a chemical light oil product and unconverted oil; The unconverted oil is subjected to a hydrocracking treatment in a hydrocracking unit (4), and the obtained hydrocracking product is mixed with the heavy oil fraction and then returned to the hydrotreating unit (2).

2. The method according to claim 1, characterized in that The operating conditions of the crude oil fractionation unit (1) include: the cut point between the light oil fraction and the heavy oil fraction is 160-200°C, preferably 170-185°C; The operating conditions of the product fractionation unit (3) include: the fraction cut point of the gas product and the chemical light oil product is 40-80°C, preferably 50-65°C; the fraction cut point of the chemical light oil product and the unconverted oil is 160-200°C, preferably 170-185°C.

3. The method according to claim 1, characterized in that The reactor in the hydrotreating unit (2) is selected from one or more of a fixed bed reactor, an ebullating bed reactor and a suspended bed reactor; The operating conditions of the hydrotreating unit (2) include: an inlet temperature of 250-420°C, a hydrogen partial pressure of 8.0-14.5 MPa, a volume space velocity of 1.0-2.0 h -1 , hydrogen oil volume ratio 500~1000Nm 3 / m 3 .

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

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

6. The method according to claim 1, characterized in that The reactor in the hydrocracking unit (4) is a fixed bed reactor or an ebullating bed reactor; When the API of the petroleum crude oil is ≮26, the reactor in the hydrocracking unit (4) is a fixed bed reactor; When the API of the petroleum crude oil is 10-26, the reactor in the hydrocracking unit (4) is an ebullating bed reactor.

7. The method according to claim 1, characterized in that The catalyst used in the hydrofining treatment includes a hydrofining catalyst; The hydrotreating 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.

8. The method according to claim 1, characterized in that The catalyst used in the hydrocracking treatment includes a hydrocracking catalyst; 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.

9. The method according to claim 1, characterized in that: The crude oil fractionation unit (1) is an atmospheric pressure fractionation tower or a vacuum fractionation tower, preferably an atmospheric pressure fractionation tower; The product fractionation unit (3) is a normal pressure fractionation tower or a reduced pressure fractionation tower, preferably a normal pressure fractionation tower.

10. A system for producing chemical materials using the method according to any one of claims 1 to 9, characterized in that: The system comprises a crude oil fractionation unit (1), a hydrofining unit (2), a product fractionation unit (3) and a hydrocracking unit (4); The crude oil fractionation unit (1) comprises a petroleum crude oil inlet, a light oil fraction outlet and a heavy oil fraction outlet; The hydrotreating unit (2) comprises a heavy oil fraction inlet, a hydrocracking product inlet and a hydrotreating product outlet; The product fractionation unit (3) comprises a hydrorefining product inlet, a gas product outlet, a chemical light oil product outlet and an unconverted oil outlet; The hydrocracking unit (4) comprises an unconverted oil inlet and a hydrocracking product outlet; The petroleum crude oil inlet of the crude oil fractionation unit (1) is connected to the petroleum crude oil source, the heavy oil fraction outlet of the crude oil fractionation unit (1) is connected to the heavy oil fraction inlet of the hydrotreating unit (2); the hydrotreating product outlet of the hydrotreating unit (2) is connected to the hydrotreating product inlet of the product fractionation unit (3); the unconverted oil outlet of the product fractionation unit (3) is connected to the unconverted oil inlet of the hydrocracking unit (4); the hydrocracking product outlet of the hydrocracking unit (4) is connected to the hydrocracking product inlet of the hydrotreating unit (2).

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