A method for producing a blending component of low-sulfur marine fuel oil from diesel raw materials

Abstract

The present invention relates to a method for producing a blending component of low-sulfur marine fuel oil from diesel raw materials. After subjecting a presulfurized hydrotreating catalyst to an accelerated deactivation treatment, the diesel raw material oil is brought into contact with the treated hydrotreating catalyst for reaction. The reaction product is separated to obtain a hydrotreated product oil, and the sulfur content of the obtained hydrotreated product oil is less than 0.01% by weight, which is a blending component of low-sulfur marine fuel oil. By using the method provided by the present invention, it is possible to process poor-quality diesel for a long period to produce a blending component of low-sulfur marine fuel oil, with low hydrogen consumption and high economy.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrocarbon raw material processing, and particularly relates to a method for producing low-sulfur marine fuel oil and its blending components from diesel raw materials. Background Art

[0002] The proportion of catalytic cracking diesel in China's diesel products is relatively high, accounting for about 1 / 3 of commercial diesel. With the increasing deterioration and heavy quality of crude oil, the quality of catalytic cracking diesel fractions has been deteriorating day by day, mainly manifested as high sulfur, nitrogen, and aromatic hydrocarbon contents, low cetane number, and poor stability. In recent years, with the wide application of high-severity catalytic cracking technologies such as catalytic cracking technology for producing more isoparaffins (MIP), the aromatic hydrocarbon content, especially the polycyclic aromatic hydrocarbon content, in MIP catalytic diesel has further increased, and the cetane number has further decreased. With the continuous enhancement of environmental awareness, the national requirements for the clean quality of ordinary diesel have been continuously upgraded, the cost of refining enterprises to produce diesel meeting the quality standards has been continuously increasing, and at the same time, the market demand for diesel has significantly decreased, highlighting the problem of diesel surplus. Therefore, it is necessary to process low-quality diesel into high-value-added products.

[0003] On the other hand, with the increasingly strict environmental requirements, the sulfur content requirements for marine fuel oil have become gradually more stringent. According to the provisions of the International Maritime Organization (IMO)'s International Convention for the Prevention of Pollution from Ships, since January 1, 2020, ships globally must use marine fuel oil with a sulfur content not higher than 0.5% by weight, which poses a great challenge to the supply of low-sulfur marine fuel oil. If excessive catalytic diesel can be used to produce blending components for low-sulfur marine fuel oil, it can not only solve the outlet of catalytic diesel and reduce processing costs, but also reduce the viscosity of marine fuel oil, improve the fluidity of fuel oil, and at the same time broaden the source of marine fuel oil.

[0004] However, during the hydrodesulfurization of catalytic diesel, with the increase in the depth of hydrodesulfurization, the aromatic hydrocarbon saturation rate in the raw material increases significantly, resulting in an increase in the reaction hydrogen consumption of the unit and a reduction in the overall economic efficiency. Therefore, it is necessary to solve the problem of how to reduce the aromatic hydrocarbon saturation reaction and increase the proportion of desulfurization reaction during the reaction process.

[0005] CN101092575A discloses a method for producing low-sulfur and low-aromatic diesel. The raw material oil is mixed with hydrogen and then enters a hydrotreating reactor, passing through a first hydrotreating reaction zone and a second hydrotreating reaction zone in sequence, and contacting with hydrofining catalyst I and hydrofining catalyst II respectively for reaction. After the reaction products are cooled and separated, the obtained liquid-phase stream enters a fractionation system, and after fractionation, a crude gasoline fraction, a light diesel fraction, and a heavy diesel fraction are obtained, and part or all of the heavy diesel fraction is returned to the hydrotreating reactor. By using the method provided by the present invention, diesel fractions with high sulfur, high nitrogen, and high metal content can be processed, and clean diesel with low sulfur and low aromatic hydrocarbons can be obtained under relatively mild operating conditions. Summary of the Invention

[0006] The present invention aims to solve the problems in the prior art that there are few blending components for low-sulfur marine fuel oil, and when processing inferior diesel with a high aromatic content, the aromatic saturation rate is too high, resulting in an increase in the reaction hydrogen consumption of the unit and low overall economic efficiency.

[0007] The sulfur compounds in diesel fractions mainly include mercaptans, disulfides, thiophenes, benzothiophenes, and dibenzothiophenes. Due to the differences in molecular size, molecular structure, the number of substituents, and the position of substituents of various sulfides, their hydrodesulfurization activities vary greatly. The reaction activities of mercaptans, disulfides, and thiophenes are much higher than those of dibenzothiophene sulfides, and they can be removed under mild hydrotreating conditions; while for dibenzothiophene sulfides with substituents at the ortho position of the sulfur atom, due to the steric hindrance effect, their hydrodesulfurization activity is the lowest, and the hydrodesulfurization rate is also very low under relatively harsh reaction conditions. However, if the requirements for low-sulfur diesel are to be met, these difficult-to-react polysubstituted dibenzothiophene sulfides must be removed. But during the hydrodesulfurization of high-aromatic inferior diesel, as the depth of hydrodesulfurization increases, the aromatic saturation rate in the feedstock will also increase significantly, resulting in a significant increase in the chemical hydrogen consumption of the unit.

[0008] The inventors of the present invention further studied in depth and found that: the first-ring hydrogenation saturation reaction of polycyclic aromatic hydrocarbons usually has a larger rate constant than the hydrogenation saturation reaction of monocyclic aromatic hydrocarbons, that is, the hydrogenation of the first ring of polycyclic aromatic hydrocarbons is easier than the hydrogenation saturation of monocyclic aromatic hydrocarbons; the desulfurization reaction is controlled by kinetics, and as the reaction temperature increases, the desulfurization rate gradually increases; while the aromatic saturation reaction is a strongly exothermic reaction and is controlled by both kinetics and thermodynamics. Increasing the reaction temperature will lead to an increase in the reaction rate but a decrease in the reaction depth; in addition, the deactivation rates of the active desulfurization and aromatic saturation activities of the hydrotreating catalyst are different, indicating that different types of active centers have different desulfurization selectivities. In the present invention, polycyclic aromatic hydrocarbons refer to the general term of bicyclic aromatic hydrocarbons and aromatic hydrocarbons with three or more rings.

[0009] Based on the above research, the present invention provides a method for producing blending components of low-sulfur marine fuel oil from diesel raw materials, including:

[0010] (1) Accelerated deactivation stage: contacting the presulfided hydrotreating catalyst with the accelerated deactivation feedstock for accelerated deactivation treatment. The distillation range of the accelerated deactivation feedstock is 150 - 400 °C, and the polycyclic aromatic hydrocarbon content is 40 - 80 wt%. The accelerated deactivation reaction conditions are: average reaction temperature 330 - 370 °C, liquid hourly space velocity 0.5 - 4.0 h -1 , hydrogen-oil volume ratio 300 - 1000, hydrogen partial pressure 5.0 - 8.0 MPa;

[0011] (2) Stable production stage: The diesel raw material oil reacts in the presence of hydrogen by contacting with the hydrotreating catalyst after being treated in step (1). The reaction products are separated to obtain hydroprocessed oil. The sulfur content of the obtained hydroprocessed oil is less than 0.01 wt%, which is a blending component for low-sulfur marine fuel oil.

[0012] In one embodiment of the present invention, the initial boiling point of the obtained hydroprocessed oil is 180 - 220 °C.

[0013] In the present invention, the boiling range of the diesel raw material oil is 150 - 400 °C, the total aromatic hydrocarbon content is 60 - 90 mass%, and the polycyclic aromatic hydrocarbon content is 40 - 80 mass%.

[0014] In one embodiment of the present invention, the diesel raw material oil is selected from one or more of catalytic cracking light cycle oil, catalytic cracking heavy cycle oil, straight-run diesel oil of naphthenic crude oil, coking diesel oil of naphthenic crude oil, diesel fraction of coal direct liquefaction oil, and diesel fraction of coal tar.

[0015] In one embodiment of the present invention, the distillation range of the acceleration deactivation raw material is 180 - 370 °C, and the polycyclic aromatic hydrocarbon content is 50 - 80 wt%.

[0016] In one embodiment of the present invention, the diesel raw material oil can be used as the acceleration deactivation raw material.

[0017] In the present invention, the pre-sulfurized hydrotreating catalyst is first contacted with the acceleration deactivation raw material in a hydrogen environment, and acceleration deactivation is carried out at a relatively high reaction temperature to rapidly reduce the aromatic saturation activity of the hydrotreating catalyst; then the diesel raw material oil is switched, and normal production is carried out under relatively mild reaction conditions, so as to achieve a certain depth of desulfurization while having as low an aromatic saturation rate as possible.

[0018] In a preferred case, the acceleration deactivation reaction conditions: the average reaction temperature is 340 - 365 °C, the liquid hourly space velocity is 0.8 - 3.0 h -1 , the hydrogen-oil volume ratio is 300 - 600, and the hydrogen partial pressure is 5.0 - 8.0 MPa.

[0019] In one embodiment of the present invention, in step (1), based on the polycyclic aromatic hydrocarbon saturation rate of the initial hydroprocessed oil, when the polycyclic aromatic hydrocarbon saturation rate of the hydroprocessed oil decreases by 10% - 20%, the acceleration deactivation stage ends; the initial hydroprocessed oil refers to the hydroprocessed oil obtained after the replacement of the acceleration deactivation raw material is completed and the device has been operating for 1 - 2 hours.

[0020] In a preferred case, based on the polycyclic aromatic hydrocarbon saturation rate of the initial hydroprocessed oil, when the polycyclic aromatic hydrocarbon saturation rate of the hydroprocessed oil decreases by 12% - 18%, the acceleration deactivation stage ends.

[0021] In the present invention, the saturation rate of polycyclic aromatic hydrocarbons is defined as follows:

[0022] Saturation rate of polycyclic aromatic hydrocarbons = (A df - A dp ) / A df * 100%

[0023] Wherein: A df — Content of polycyclic aromatic hydrocarbons in the raw material, mass %

[0024] A dp — Content of polycyclic aromatic hydrocarbons in the hydrogenated product oil, mass %

[0025] The "content of polycyclic aromatic hydrocarbons" in the present invention refers to the sum of the mass fractions of aromatic hydrocarbons with two or more rings including the bicyclic aromatic hydrocarbons themselves in the mass spectrometry composition data obtained by mass spectrometry (analysis method SH / T-0606).

[0026] In one embodiment of the present invention, the hydrotreating catalyst contains a carrier and a hydrogenation metal active component supported on the carrier; based on the total weight of the hydrotreating catalyst, the content of the hydrogenation metal active component is 12 to 45% by weight in terms of oxide.

[0027] Preferably, the carrier is selected from one or more of γ-alumina, silica, and alumina-silica.

[0028] Preferably, the hydrogenation metal active component of the hydrotreating catalyst contains cobalt and molybdenum.

[0029] In one embodiment of the present invention, the reaction conditions in the stable production stage: the average reaction temperature is 280 to 365 °C, the liquid hourly space velocity is 0.5 to 3.0 h -1 , the hydrogen-oil volume ratio is 300 to 1000, and the hydrogen partial pressure is 4.0 to 10.0 MPa;

[0030] Preferred reaction conditions in the stable production stage: the average reaction temperature is 300 to 350 °C, the liquid hourly space velocity is 0.5 to 2.5 h -1 , the hydrogen-oil volume ratio is 300 to 600, and the hydrogen partial pressure is 5.0 to 8.0 MPa.

[0031] The present invention controls the hydrogenation depth by controlling the process parameters in the stable production stage, further promotes the hydrodesulfurization reaction, and avoids the hydrogenation saturation of aromatics to cycloalkanes as much as possible, that is, while reducing the content of impurities such as sulfur and nitrogen in diesel feed oil, the occurrence of aromatic hydrogenation saturation reaction is reduced. The hydrogenated oil obtained by the present invention is rich in aromatics, and the sulfur content is less than 0.01% by weight. The hydrogenated oil is used as a high-quality blending component of low-sulfur marine fuel oil. On the one hand, it can also reduce the viscosity of marine fuel oil and improve the fluidity of marine fuel oil. On the other hand, as a high-quality low-sulfur blending component, it can increase the proportion of other high-sulfur blending components of marine fuel oil, thereby broadening the source of marine fuel oil.

[0032] Features of the present invention:

[0033] (1) The present invention can process diesel fuel oil with high aromatic content, and has high desulfurization selectivity while maintaining a high desulfurization rate. When the desulfurization rate reaches more than 90%, the saturation rate of polycyclic aromatic hydrocarbons is less than 50%, which significantly reduces the aromatic hydrogenation saturation rate and reduces the process chemical hydrogen consumption. Compared with the conventional hydrorefining process, the present invention can reduce the aromatic saturation rate by more than 5% and the polycyclic aromatic hydrocarbon saturation rate by more than 20%, thereby effectively reducing hydrogen consumption.

[0034] (2) The method provided by the present invention processes low-quality diesel feedstock oil with high sulfur and high aromatic content to produce high-quality blending components for low-sulfur marine fuel oil, which can not only solve the problem of diesel overcapacity, but also broaden the source of marine fuel oil and effectively improve the economic benefits of refineries. DETAILED DESCRIPTION

[0035] The present invention will be further described below in conjunction with embodiments, but the present invention is not limited thereto.

[0036] Table 1 lists the properties of the treated diesel feedstocks.

[0037] Table 2 lists the main components of the hydroprocessing catalysts used in the examples and comparative examples of the present invention. The RS-2200 catalyst with a commercial brand is produced by Sinopec Catalyst Branch, and the hydroprocessing catalyst without a commercial brand is obtained by a conventional fixed bed supported hydrogenation catalyst preparation method.

[0038] In the comparative examples and examples listed below, each hydroprocessing catalyst was subjected to a presulfidation treatment, and the method and conditions of the presulfidation treatment were the same.

[0039] Comparative Example 1

[0040] Diesel feedstock A is mixed with hydrogen and reacted with a presulfurized hydrotreating catalyst C. The reaction product is separated to obtain hydrogenated oil. The hydrogenation reaction conditions and the properties of the hydrogenated oil are shown in Table 3.

[0041] As can be seen from Table 3, the sulfur content of the hydrogenated product oil is 19 μg / g, the polycyclic aromatic hydrocarbon (PAH) content is 10.7% by mass, the saturation rate of PAHs is 80.3%, the total aromatic hydrocarbon saturation rate is 14.7%, and the chemical hydrogen consumption is 2.1%.

[0042] Example 1

[0043] Accelerated deactivation stage: The presulfurized hydrotreating catalyst C was contacted with the accelerated deactivation feedstock (diesel feedstock A) for accelerated deactivation treatment. The reaction conditions for accelerated deactivation were as follows: average reaction temperature 360 °C, liquid hourly space velocity 2.0 h -1 , hydrogen-oil volume ratio 800, hydrogen partial pressure 6.4 MPa. The reaction product was separated to obtain the hydrogenated product oil. After replacement with the accelerated deactivation feedstock and running for 1 hour, the hydrogenated product oil obtained was used as the initial hydrogenated product oil. The PAH content in the initial hydrogenated product oil was 7.6% by mass, and the saturation rate of PAHs was 86%. After running for 30 h, the PAH content in the hydrogenated product oil was 38.1% by mass, and the saturation rate of PAHs was 70%, that is, the saturation rate of PAHs in the hydrogenated product oil decreased by 16%, and the accelerated deactivation stage ended. The reaction conditions were adjusted to those of the stable production stage. The specific reaction conditions and product properties are shown in Table 3.

[0044] As can be seen from Table 3, the sulfur content of the obtained hydrogenated product oil is 23 μg / g, the PAH content is 28.3% by mass, which is a blending component for low-sulfur marine fuel oil; the saturation rate of PAHs in the hydrogenated product oil is 48.0%, the total aromatic hydrocarbon saturation rate is 9.0%, and the chemical hydrogen consumption is 1.7%.

[0045] Compared with Comparative Example 1, under substantially the same stable production reaction conditions, the desulfurization selectivity of this example increased significantly, and the chemical hydrogen consumption at the same desulfurization depth decreased by 19%.

[0046] Comparative Example 2

[0047] Diesel feedstock B was mixed with hydrogen and contacted with the hydrotreating catalyst D that had been in operation for more than one year for reaction. The reaction product was separated to obtain the hydrogenated product oil. The hydrogenation reaction conditions and the properties of the hydrogenated product oil are shown in Table 4.

[0048] As can be seen from Table 4, the sulfur content of the obtained hydrogenated product oil is 95 μg / g, the PAH content is 16.5% by mass, the saturation rate of PAHs in the hydrogenated product oil is 71.5%, the total aromatic hydrocarbon saturation rate is 27.2%, and the chemical hydrogen consumption is 2.4%.

[0049] Since it has been in operation for more than one year, there is a lot of carbon deposition on the hydrotreating catalyst D. The reaction temperature needs to be increased to obtain a comparable desulfurization rate. Although the polycyclic aromatic hydrocarbon saturation rate has decreased, the chemical hydrogen consumption is still relatively high.

[0050] Example 2

[0051] Accelerated deactivation stage: The pre-sulfurized hydrotreating catalyst D is contacted with the accelerated deactivation feedstock (diesel feedstock B) for accelerated deactivation treatment. The reaction conditions for accelerated deactivation are as follows: average reaction temperature 355 °C, liquid hourly space velocity 2.5 h -1 , hydrogen-oil volume ratio 800, hydrogen partial pressure 6.4 MPa. The reaction products are separated to obtain the hydrogenated product oil. After the replacement with the accelerated deactivation feedstock is completed, the hydrogenated product oil obtained after 1 hour of operation is used as the initial hydrogenated product oil. The content of polycyclic aromatic hydrocarbons in the initial hydrogenated product oil is 9.8% by mass, and the polycyclic aromatic hydrocarbon saturation rate is 83%. After operating for 32 h, the content of polycyclic aromatic hydrocarbons in the hydrogenated product oil is 18.5% by mass, and the polycyclic aromatic hydrocarbon saturation rate is 68%, that is, the polycyclic aromatic hydrocarbon saturation rate of the hydrogenated product oil decreases by 15%, and the accelerated deactivation stage ends. The reaction conditions are adjusted to those of the stable production stage, and the specific reaction conditions and product properties are shown in Table 4.

[0052] As can be seen from Table 4, the sulfur content of the obtained hydrogenated product oil is 88 μg / g, the content of polycyclic aromatic hydrocarbons is 28.3% by mass, which is a blending component for low-sulfur marine fuel oil; the polycyclic aromatic hydrocarbon saturation rate of the hydrogenated product oil is 51.1%, the total aromatic hydrocarbon saturation rate is 23.0%, and the chemical hydrogen consumption is 1.87%.

[0053] Compared with Comparative Example 2, the method provided by the present invention can obtain a comparable desulfurization rate while reducing the aromatic hydrocarbon saturation rate and reducing the chemical hydrogen consumption by 20% under the premise that the reaction temperature is reduced by 5 °C in the stable production stage.

[0054] Comparative Example 3

[0055] Accelerated deactivation stage: The pre-sulfurized hydrotreating catalyst D is contacted with the accelerated deactivation feedstock (diesel feedstock B) for accelerated deactivation treatment. The reaction conditions for accelerated deactivation are as follows: average reaction temperature 362 °C, liquid hourly space velocity 1.2 h -1, with a hydrogen-oil volume ratio of 800 and a hydrogen partial pressure of 6.4 MPa, the reaction products were separated to obtain the hydrogenated product oil. After replacing with the accelerated deactivation feedstock and running for 1 hour, the obtained hydrogenated product oil was used as the initial hydrogenated product oil. The content of polycyclic aromatic hydrocarbons in the initial hydrogenated product oil was 6.4% by mass, and the saturation rate of polycyclic aromatic hydrocarbons was 89%. After running for 48 h, the content of polycyclic aromatic hydrocarbons in the hydrogenated product oil was 20.8% by mass, and the saturation rate of polycyclic aromatic hydrocarbons was 64%, that is, the saturation rate of polycyclic aromatic hydrocarbons in the hydrogenated product oil decreased by 25%, and the accelerated deactivation stage ended. The reaction conditions were adjusted to those in the stable production stage, and the specific reaction conditions and product properties are shown in Table 4.

[0056] As can be seen from Table 4, the sulfur content of the obtained hydrogenated product oil was 80 μg / g, and the content of polycyclic aromatic hydrocarbons was 29% by mass; the saturation rate of polycyclic aromatic hydrocarbons in the hydrogenated product oil was 49.9%, the total aromatic hydrocarbon saturation rate was 22%, and the chemical hydrogen consumption was 2.1%.

[0057] Compared with Example 2, the accelerated deactivation in Comparative Example 3 exceeded the preferred range. Therefore, higher reaction temperature and lower volume space velocity were required to ensure that the sulfur content of the product was less than 100 μg / g. However, side reactions such as cracking increased at this time, and the chemical hydrogen consumption also increased.

[0058] Table 1

[0059] Feedstock A B <![CDATA[Density (20 °C) / (g / cm 3 )]]> 0.9347 0.9584 Sulfur content / (μg / g) 2300 6500 Total aromatics / mass % 80.7 85.6 Polycyclic aromatics / mass % 54.4 57.9 Distillation range (ASTM D-86) / °C Initial boiling point 176 213 50％ 265 290 Final boiling point 335 360

[0060] Table 2

[0061]

[0062]

[0063] Table 3

[0064] Number Comparative Example 1 Example 1 Reaction conditions for stable production Hydrogen partial pressure, MPa 6.4 6.4 Reaction temperature, °C 330 335 <![CDATA[Liquid hourly space velocity, h -1 > 1.0 1.0 <![CDATA[Hydrogen-oil volume ratio, Nm 3 / m 3 > 800 800 Properties of hydrogenated product oil Initial boiling point, °C 180 180 Sulfur content, μg / g 19 23 Polycyclic aromatics, mass % 10.7 28.3 Total aromatics, mass % 68.8 73.4 Saturation rate of polycyclic aromatics, % 80.3 48.0 Saturation rate of total aromatics, % 14.7 9.0 Chemical hydrogen consumption, wt% 2.1 1.7

[0065] Table 4

[0066]

[0067]

Claims

1. A method for producing a blending component of low-sulfur marine fuel oil from diesel raw materials, comprising: (1) Accelerated deactivation stage: The presulfurized hydrotreating catalyst is contacted with the accelerated deactivation feedstock for accelerated deactivation treatment. The distillation range of the accelerated deactivation feedstock is 150 - 400 °C, and the polycyclic aromatic hydrocarbon content is 40 - 80 wt%. The accelerated deactivation reaction conditions are as follows: the average reaction temperature is 330 - 370 °C, the liquid hourly space velocity is 0.5 - 4.0 h -1 , the hydrogen-to-oil volume ratio is 300 - 1000, and the hydrogen partial pressure is 4.0 - 10.0 MPa. Based on the polycyclic aromatic hydrocarbon saturation rate of the initial hydrogenated product oil, when the polycyclic aromatic hydrocarbon saturation rate of the hydrogenated product oil decreases by 10% - 20%, the accelerated deactivation stage ends. The initial hydrogenated product oil refers to the hydrogenated product oil obtained after the replacement of the accelerated deactivation feedstock is completed and the unit has been operating for 1 - 2 hours; (2) Stable production stage: The diesel raw material oil reacts with the hydrotreating catalyst after being treated in step (1) in the presence of hydrogen. The reaction product is separated to obtain hydroprocessed oil. The sulfur content of the obtained hydroprocessed oil is less than 0.01% by weight, which is a blending component of low-sulfur marine fuel oil.

2. The method according to claim 1, characterized in that The boiling range of the diesel raw material oil is 150 - 400 °C, the total aromatic hydrocarbon content is 60 - 90% by mass, and the polycyclic aromatic hydrocarbon content is 40 - 80% by mass.

3. The method according to claim 1 or 2, characterized in that, The diesel raw material oil is selected from one or more of catalytic cracking light cycle oil, catalytic cracking heavy cycle oil, straight-run diesel oil of naphthenic crude oil, coking diesel oil of naphthenic crude oil, diesel fraction of coal direct liquefaction oil, and diesel fraction of coal tar.

4. The method according to claim 1, characterized in that Accelerated deactivation reaction conditions: average reaction temperature 340~365°C, liquid hourly space velocity 0.8~3.0 h -1 , hydrogen-oil volume ratio 300~600, hydrogen partial pressure 5.0~8.0 MPa.

5. The method according to claim 1, wherein The distillation range of the acceleration deactivation raw material is 180 - 370 °C, and the polycyclic aromatic hydrocarbon content is 50 - 80% by weight.

6. The method according to claim 1, characterized in that, In step (1), based on the polycyclic aromatic hydrocarbon saturation rate of the initial hydroprocessed oil, when the polycyclic aromatic hydrocarbon saturation rate of the hydroprocessed oil decreases by 12% - 18%, the acceleration deactivation stage ends.

7. The method according to claim 1, characterized in that, The hydrotreating catalyst contains a carrier and a hydro-metallic active component supported on the carrier; based on the total weight of the hydrotreating catalyst, the content of the hydro-metallic active component is 12 - 45% by weight in terms of oxide.

8. The method according to claim 7, characterized in that, The hydro-metallic active component of the hydrotreating catalyst contains cobalt and molybdenum.

9. The method according to claim 1, wherein Reaction conditions in the stable production stage: average reaction temperature 280~365°C, liquid hourly space velocity 0.5~3.0 h -1 , hydrogen-oil volume ratio 300~1000, hydrogen partial pressure 4.0~10.0 MPa.

10. The method according to claim 1, characterized in that Reaction conditions during the stable production stage: average reaction temperature 300 - 350 °C, liquid hourly space velocity 0.5 - 2.5 h -1 , hydrogen-to-oil volume ratio 300 - 600, hydrogen partial pressure 5.0 - 8.0 MPa.

Images