Marine fuel oil and its preparation method

Abstract

The present invention relates to the field of marine fuel oil, and discloses a marine fuel oil and a preparation method thereof. The marine fuel oil comprises 10 - 50 wt% of base oil, 11 - 53 wt% of low-sulfur atmospheric and vacuum residue, 9 - 30 wt% of aromatic hydrocarbon component and 10 - 50 wt% of low-sulfur distillate; the base oil is selected from the atmospheric tower bottom oil of the ebullated bed residue hydrotreating process and / or the middle section heavy wax oil of the vacuum tower of the ebullated bed residue hydrotreating process; the aromatic hydrocarbon component is selected from at least one of catalytic slurry oil with an end boiling point ≤ 480 °C, catalytic cycle oil, and catalytic diesel; the sulfur content of the low-sulfur distillate is ≤ 0.5 wt%, and it is selected from at least one of residue plus wax oil, straight-run wax oil, V hydrorefined wax oil, and hydro-upgrading heavy cracking tar. The present invention can turn the atmospheric tower bottom oil of the ebullated bed residue hydrotreating process and the middle section heavy wax oil of the vacuum tower of the ebullated bed residue hydrotreating process into valuable resources, and obtain a high-quality low-sulfur marine fuel oil that can meet the requirements of the compatibility index, sulfur content index, viscosity index and other full performance indexes of low-sulfur marine fuel oil, and has good application prospects.

Description

Technical Field

[0001] The present invention relates to the technical field of marine fuel oil, and particularly relates to a marine fuel oil and a preparation method thereof. Background Art

[0002] Crude oil can be divided into low-sulfur crude oil with a sulfur content < 0.5 wt%, sulfur-containing crude oil with a sulfur content of 0.5 - 2 wt%, and high-sulfur crude oil with a sulfur content > 2% according to the sulfur content. The residue obtained by the atmospheric and vacuum distillation of low-sulfur crude oil is low-sulfur atmospheric and vacuum residue, and the residue obtained by the atmospheric and vacuum distillation of high-sulfur crude oil is high-sulfur atmospheric and vacuum residue with a sulfur content of 4 - 5 wt%. The high-sulfur atmospheric and vacuum residue can be subjected to thermal cracking and hydrofining treatment in a fluidized-bed residue hydrotreating reactor. The reaction products then enter an atmospheric column for atmospheric distillation. The bottom oil of the atmospheric column drawn therefrom enters a vacuum column for further vacuum distillation. Middle light wax oil with a distillation range of 350 - 470 °C and middle heavy wax oil with a distillation range of 380 - 510 °C can be sequentially drawn from the vacuum column, and the remaining fraction is unconverted oil, which is discharged from the bottom of the vacuum column.

[0003] Low-sulfur atmospheric and vacuum residue is a common blending component of marine fuel oil. Compared with low-sulfur atmospheric and vacuum residue, the compatibility index of the bottom oil of the atmospheric column in the fluidized-bed residue hydrotreating process is ≥ 4 levels, and the compatibility of the middle heavy wax oil in the vacuum column of the fluidized-bed residue hydrotreating process is ≥ 3 levels. The compatibility and stability of the bottom oil of the atmospheric column and the middle heavy wax oil are poor, and the compatibility with light fractions is weak. Therefore, it is difficult to use the bottom oil of the atmospheric column and the middle heavy wax oil to prepare marine fuel oil that meets national standards. Summary of the Invention

[0004] The purpose of the present invention is to solve the problem in the prior art that it is difficult to use the bottom oil of the atmospheric column in the fluidized-bed residue hydrotreating process and the middle heavy wax oil in the vacuum column of the fluidized-bed residue hydrotreating process to prepare marine fuel oil, and to provide a marine fuel oil and a preparation method thereof.

[0005] To achieve the above purpose, in the first aspect of the present invention, a marine fuel oil is provided. Based on the total amount of the marine fuel oil, the marine fuel oil includes 10 - 50 wt% of base oil, 11 - 53 wt% of low-sulfur atmospheric and vacuum residue, 9 - 30 wt% of aromatic hydrocarbon components, and 10 - 50 wt% of low-sulfur fractions;

[0006] Among them, the base oil is selected from the bottom oil of the atmospheric column in the fluidized-bed residue hydrotreating process and / or the middle heavy wax oil in the vacuum column of the fluidized-bed residue hydrotreating process; the aromatic hydrocarbon components are selected from at least one of catalytic oil slurry, catalytic recycle oil, and catalytic diesel; among them, the final boiling point of the catalytic oil slurry ≤ 480 °C; the sulfur content of the low-sulfur fraction ≤ 0.5 wt%, and it is selected from at least one of slurry plus wax oil, straight-run wax oil, V hydrofined wax oil, and hydro-upgrading heavy cracking tar.

[0007] The second aspect of the present invention provides a method for preparing marine fuel oil, the method comprising: mixing a base oil, a low-sulfur atmospheric and vacuum residue, an aromatic component, a low-sulfur distillate, and an optional antioxidant to obtain the marine fuel oil.

[0008] Through the above technical solution, the present invention uses an aromatic component, a low-sulfur atmospheric and vacuum residue, a low-sulfur distillate, and an optional antioxidant to blend the bottom oil of the atmospheric column of the ebullated bed residue hydrotreating process and the middle-section heavy wax oil of the vacuum column of the ebullated bed residue hydrotreating process, which can turn the bottom oil of the atmospheric column of the ebullated bed residue hydrotreating process and the middle-section heavy wax oil of the vacuum column of the ebullated bed residue hydrotreating process from waste into valuable products, obtaining high-quality low-sulfur marine fuel oil that meets the requirements of the compatibility index, sulfur content index, viscosity index, and other full-performance indicators of low-sulfur marine fuel oil, and has good application prospects. Detailed Embodiments

[0009] In the ranges disclosed herein, the endpoints and any values are not limited to the exact ranges or values, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, between the endpoint values of each range, between the endpoint values of each range and individual point values, and between individual point values, they can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be regarded as specifically disclosed herein.

[0010] Among them, in the present invention, unless otherwise specified, the distillation range refers to the temperature range from the 10% distillation temperature to the 90% distillation temperature. Among them, the 10% distillation temperature and the 90% distillation temperature refer to the temperatures when the distillation volumes reach 10% and 90% of the sample respectively.

[0011] The first aspect of the present invention provides a marine fuel oil, wherein, based on the total amount of the marine fuel oil, the marine fuel oil comprises 10 - 50 wt% of a base oil, 11 - 53 wt% of a low-sulfur atmospheric and vacuum residue, 9 - 30 wt% of an aromatic component, and 10 - 50 wt% of a low-sulfur distillate;

[0012] Among them, the base oil is selected from the bottom oil of the atmospheric column of the ebullated bed residue hydrotreating process and / or the middle-section heavy wax oil of the vacuum column of the ebullated bed residue hydrotreating process; the aromatic component is selected from at least one of catalytic slurry oil, catalytic recycle oil, and catalytic diesel; among them, the final boiling point of the catalytic slurry oil ≤ 480 °C; the sulfur content of the low-sulfur distillate ≤ 0.5 wt%, and it is selected from at least one of coker wax oil, straight-run wax oil, V hydrofined wax oil, and hydro-upgrading heavy cracking tar.

[0013] Compatibility, sulfur content, and viscosity are three very crucial technical indicators for marine fuel oil. In the present invention, the low-sulfur atmospheric and vacuum residue and aromatic components act synergistically to reduce the compatibility index of the bottom oil of the atmospheric column in the ebullated-bed residue hydrotreating process and / or the middle-stage heavy wax oil of the vacuum column in the ebullated-bed residue hydrotreating process. Subsequently, when combined with low-sulfur components, a low-sulfur marine fuel oil can be obtained whose compatibility, sulfur content, and viscosity indicators all meet the national standards.

[0014] In a preferred embodiment, based on the total amount of the marine fuel oil, the marine fuel oil comprises 20 - 45 wt% of base oil, 11 - 25 wt% of low-sulfur atmospheric and vacuum residue, 15 - 25 wt% of aromatic components, and 25 - 45 wt% of low-sulfur fractions.

[0015] Among them, in the present invention, when the contents of the base oil, low-sulfur atmospheric and vacuum residue, aromatic components, and low-sulfur fractions are within the above ranges, the comprehensive performance of the prepared marine fuel oil is better.

[0016] In a preferred embodiment, the distillation range of the bottom oil of the atmospheric column in the ebullated-bed residue hydrotreating process is 356 - 482 °C; among them, the compatibility of the bottom oil of the atmospheric column in the ebullated-bed residue hydrotreating process is ≥ 4 grades, and the sulfur content is 0.5 - 0.8 wt%.

[0017] In a preferred embodiment, the distillation range of the middle-stage heavy wax oil of the vacuum column in the ebullated-bed residue hydrotreating process is 380 - 510 °C; among them, the compatibility of the middle-stage heavy wax oil of the vacuum column in the ebullated-bed residue hydrotreating process is ≥ 3 grades, and the sulfur content is 0.2 - 0.45 wt%.

[0018] In a preferred embodiment, the atmospheric and vacuum residue in the low-sulfur atmospheric and vacuum residue has the well-known meaning in the art, and the present invention does not make special limitations on it. The sulfur content of the low-sulfur atmospheric and vacuum residue is ≤ 1.5 wt%, preferably ≤ 1 wt%.

[0019] In a preferred embodiment, the catalytic slurry, catalytic diesel, and catalytic recycle oil come from the catalytic cracking unit of a refinery. The three components have the well-known meaning in the art, and the present invention does not make special limitations on them.

[0020] Generally, the residue oil discharged from the bottom of the catalytic cracking unit, which is the catalytic slurry, has a distillation range of 394 - 500 °C. The inventors of the present invention have found through research that by further fractionating the catalytic slurry and separating the fraction with an end boiling point below 480 °C, and using the fraction with an end boiling point below 480 °C to blend the base oil in the present invention, a low-sulfur marine fuel oil meeting the national standards can be prepared, thereby increasing the additional economic value of the catalytic slurry.

[0021] In a preferred embodiment, the content of Si + Al after solid removal of the catalytic slurry oil with an end boiling point ≤ 480 °C is ≤ 200 ppm, the aromatic hydrocarbon content is 90 - 95 wt%, the sulfur content is ≤ 0.6 wt%, and the kinematic viscosity at 50 °C is 220 - 240 mm2 / s. Among them, the present invention does not make special limitations on solid removal, and it is preferred to use an inorganic membrane for solid removal.

[0022] In a preferred embodiment, the distillation range of the catalytic recycle oil is 362 - 425 °C, the aromatic hydrocarbon content is 84 - 88 wt%, the sulfur content is ≤ 0.6 wt%, and the kinematic viscosity at 50 °C is 11 - 15 mm2 / s.

[0023] In a preferred embodiment, the distillation range of the catalytic diesel is 224 - 313 °C, the aromatic hydrocarbon content is 80 - 85 wt%, the sulfur content is ≤ 0.4 wt%, and the kinematic viscosity at 50 °C is 2 - 3 mm2 / s.

[0024] In a preferred embodiment, the aromatic hydrocarbon component is catalytic diesel, and the content of the catalytic diesel is 10 - 20 wt%.

[0025] In a preferred embodiment, the aromatic hydrocarbon component is a mixture of catalytic diesel and catalytic slurry oil and / or catalytic recycle oil; among them, based on the total amount of the aromatic hydrocarbon component, the content of catalytic diesel is 15 - 50 wt%, preferably 25 - 35 wt%.

[0026] Among them, in the present invention, the inventors of the present invention have found through research that after mixing catalytic diesel with catalytic slurry oil and / or catalytic recycle oil in the above proportions, it can not only play a role in reducing the compatibility of the base oil, but also further reduce the sulfur content of the marine fuel oil.

[0027] In a preferred embodiment, the residue plus wax oil is a fraction with a distillation range of 330 - 450 °C taken from the atmospheric column of the ebullated bed residue hydrotreating process; among them, the sulfur content of the residue plus wax oil is 0.2 - 0.4 wt%.

[0028] In a preferred embodiment, the straight-run wax oil is a fraction with a distillation range of 316 - 426 °C taken from the crude oil atmospheric and vacuum column; among them, the sulfur content of the straight-run wax oil is 0.2 - 0.35 wt%.

[0029] In a preferred embodiment, the V hydrofined wax oil is a fraction with a distillation range of 325 - 527 °C taken from the wax oil hydrofining unit; among them, the sulfur content of the V hydrofined wax oil is 0.09 - 0.2 wt%.

[0030] In a preferred embodiment, the hydro-upgrading heavy cracked tar (hydro-upgrading PFO) is a fraction with a distillation range of 250-380 °C taken from an ethylene cracking tar hydrogenation unit; wherein, the sulfur content of the hydro-upgrading heavy cracked tar is 0.09-0.2 wt%, and the asphaltene content is ≤5 wt%.

[0031] In a preferred embodiment, the low-sulfur fraction is V hydrofined wax oil and / or hydro-upgrading heavy cracked tar.

[0032] Wherein, in the present invention, when the low-sulfur fraction is a mixture of V hydrofined wax oil and / or hydro-upgrading heavy cracked tar, the comprehensive performance of the prepared marine fuel oil is better.

[0033] In a preferred embodiment, the marine fuel oil further comprises 110-280 ppm, preferably 120-180 ppm of an antioxidant, and the antioxidant is selected from 44PD.

[0034] In the present invention, antioxidant 44PD, also known as N,N'-di-sec-butyl-p-phenylenediamine. The addition of a trace amount of antioxidant can further improve the high-temperature stability of the low-sulfur marine fuel oil. Among them, the content of the antioxidant is equal to the ratio of the mass of the antioxidant to the total mass of the low-sulfur marine fuel oil.

[0035] The second aspect of the present invention provides a method for preparing a marine fuel oil, the method comprising: mixing a base oil, a low-sulfur atmospheric and vacuum residue, an aromatic component, a low-sulfur fraction and an optional antioxidant to obtain a marine fuel oil.

[0036] In a preferred embodiment, the operating conditions of the mixing include: the mixing temperature is 40-90 °C, preferably 60-85 °C; the stirring speed of the mixing is 80-200 r / min, preferably 150-200 r / min; the mixing time is 20-50 min, preferably 30-40 min.

[0037] In a preferred embodiment, the method comprises: first mixing the base oil with the low-sulfur atmospheric and vacuum residue and the aromatic component for the first time, and then adding the low-sulfur fraction and the optional antioxidant for the second time to obtain a marine fuel oil.

[0038] In a preferred embodiment, the operating conditions of the first mixing include: the primary mixing temperature is 55-90 °C, preferably 60-75 °C; the stirring speed of the primary mixing is 80-200 r / min, preferably 100-150 r / min; the primary mixing time is 10-30 min, preferably 10-20 min;

[0039] The operating conditions for the second mixing include: the secondary mixing temperature is 60 - 90°C, preferably 65 - 85°C; the stirring speed for the secondary mixing is 100 - 200 r / min, preferably 140 - 180 r / min; the secondary mixing time is 5 - 30 min, preferably 10 - 20 min.

[0040] In a preferred embodiment, the secondary mixing temperature is higher than the primary mixing temperature, and the stirring speed for the secondary mixing is faster than that for the primary mixing.

[0041] The present invention will be described in detail below through examples.

[0042] Base oil: The distillation range of the atmospheric tower bottom oil from the ebullated bed residue hydrotreating process is 356 - 482°C, the compatibility is grade 4, the sulfur content is 0.6 wt%, and the kinematic viscosity at 50°C is 130 mm2 / s; the distillation range of the middle heavy wax oil from the vacuum tower of the ebullated bed residue hydrotreating process is 380 - 510°C, the compatibility is grade 3, the sulfur content is 0.35 wt%, and the kinematic viscosity at 50°C is 42 mm2 / s.

[0043] Low-sulfur atmospheric and vacuum residue: The sulfur content is 0.7 wt%.

[0044] Aromatic components: The final boiling point of catalytic slurry I is ≤480°C, the Si + Al content after solid removal is 150 ppm, the aromatic content is 93 wt%, the sulfur content is 0.6 wt%, and the kinematic viscosity at 50°C is 220 mm2 / s; the distillation range of catalytic slurry II (i.e., the catalytic slurry without fractionation) is 394 - 500°C, the Si + Al content after solid removal is 180 ppm, the aromatic content is 91 wt%, the sulfur content is 0.65 wt%, and the kinematic viscosity at 50°C is 264 mm2 / s. The distillation range of catalytic recycle oil is 362 - 425°C, the aromatic content is 86 wt%, the sulfur content is 0.6 wt%, and the kinematic viscosity at 50°C is 11 mm2 / s; the distillation range of catalytic diesel is 224 - 313°C, the aromatic content is 82 wt%, the sulfur content is 0.4 wt%, and the kinematic viscosity at 50°C is 2.5 mm2 / s.

[0045] Low-sulfur fraction: V hydrofined wax oil is a fraction with a distillation range of 325 - 527°C taken from the wax oil hydrofining unit, the sulfur content is 0.12 wt%, and the kinematic viscosity at 50°C is 24 mm2 / s;

[0046] Hydro-upgrading heavy cracking tar (hydro-upgrading PFO) is a fraction with a distillation range of 250 - 380°C taken from the ethylene cracking tar hydrogenation unit, the sulfur content is 0.16 wt%, and the asphaltene content is 2 wt%.

[0047] Heavy cracked tar (i.e., heavy cracked tar without hydro-upgrading) is a fraction with a distillation range of 230 - 410 °C and a sulfur content of 0.1 wt% taken from an ethylene cracking unit.

[0048] Example 1

[0049] Put the base oil, low-sulfur atmospheric and vacuum residue, and aromatic components into a preparation storage tank, and conduct the first mixing at 65 °C with a stirring speed of 140 r / min for 20 min;

[0050] Then add the low-sulfur fraction to the preparation storage tank, and conduct the second mixing at 70 °C with a stirring speed of 170 r / min for 15 min to obtain a low-sulfur marine fuel oil.

[0051] Among them, the components and properties of the prepared low-sulfur marine fuel oil are shown in Table 1 and Table 2 respectively.

[0052] Examples 2 - 5:

[0053] Same as Example 1, except that the components of the marine fuel oil are different. The components of the marine fuel oil are shown in Table 1, and the properties of the prepared low-sulfur marine fuel oil are shown in Table 2.

[0054] Example 6:

[0055] Put the base oil, low-sulfur atmospheric and vacuum residue, aromatic components, and low-sulfur fraction into a preparation storage tank, and conduct mixing at 70 °C with a stirring speed of 170 r / min for 35 min to obtain a low-sulfur marine fuel oil.

[0056] Among them, the components and properties of the prepared low-sulfur marine fuel oil are shown in Table 1 and Table 2 respectively.

[0057] Comparative Example 1

[0058] Same as Example 1, except that catalytic slurry II of equal mass is used to replace catalytic slurry I, and the components and properties of the obtained low-sulfur marine fuel oil are shown in Table 1 and Table 2 respectively.

[0059] From the comparison of the test results of Example 1 and Comparative Example 1, it can be seen that the catalytic slurry II without fractionation cutting has a poor improvement effect on the compatibility of the base oil, and it is difficult to obtain a low-sulfur marine fuel oil with a compatibility index meeting the requirements.

[0060] Comparative Example 2

[0061] Same as Example 1, except that heavy cracked tar of equal mass is used to replace hydro-upgraded heavy cracked tar, and the components and properties of the obtained low-sulfur marine fuel oil are shown in Table 1 and Table 2 respectively.

[0062] By comparing the test results of Example 1 and Comparative Example 2, it can be seen that although the heavy cracked tar without hydro-upgrading can reduce the sulfur content index, its compatibility with the atmospheric residue oil at the bottom of the ebullated bed vacuum tower and the middle distillate heavy wax oil is poor, and the compatibility index will deteriorate significantly after blending.

[0063] Comparative Example 3

[0064] Same as Example 2, except that the low-sulfur atmospheric and vacuum residue is omitted. The components of the marine fuel oil are shown in Table 1, and the properties of the prepared low-sulfur marine fuel oil are shown in Table 2.

[0065] Comparative Example 4

[0066] Same as Example 2, except that the aromatic component is omitted. The components of the marine fuel oil are shown in Table 1, and the properties of the prepared low-sulfur marine fuel oil are shown in Table 2.

[0067] By comparing the results of Example 2 with those of Comparative Example 3 and Comparative Example 4, it can be seen that when there is only the aromatic component or only the low-sulfur atmospheric and vacuum residue, the compatibility index of the prepared low-sulfur marine fuel oil cannot meet the national standard requirements. The synergistic effect of the aromatic component and the atmospheric and vacuum residue can not only reduce the compatibility index of the atmospheric residue oil at the bottom of the ebullated bed residue hydrotreating vacuum tower and the middle distillate heavy wax oil, but also adjust the kinematic viscosity at 50 °C and the sulfur content to meet the product index requirements of low-sulfur marine fuel oil.

[0068] Table 1

[0069]

[0070] Test Example 1

[0071] The compatibility, sulfur content and viscosity at 50 °C of the marine fuel oils in Examples 1-6 and Comparative Examples 1-4 were tested, and the test results are shown in Table 2:

[0072] Table 2

[0073]

[0074]

[0075] Note: The test method for compatibility in Table 1 is ASTM D4740-20, the test method for sulfur content is GB / T 17040, and the test method for viscosity is GB / T11137. According to the regulations of GB / T 17411-2015, the compatibility of marine fuel oil ≤ 2 levels, sulfur content ≤ 0.50 wt%, viscosity (50 °C) is 100-180 mm 2 / s.

[0076] Test Example 2

[0077] Comprehensively test the performance indicators of the marine fuel oil in Example 1, and the test results are shown in Table 3 as follows:

[0078] Table 3

[0079]

[0080]

[0081] It can be seen from Table 3 that the present invention can obtain a low-sulfur marine fuel oil meeting the standards by using low-sulfur atmospheric and vacuum residue, aromatic components and low-sulfur distillate to regulate the base oil.

[0082] Test Example 3

[0083] Refer to Example 1 to prepare three portions of low-sulfur marine fuel oil. The difference is that during the second mixing, 50 ppm, 100 ppm, and 120 ppm of antioxidant 44PD (purchased from Anhui Weichi Chemical Co., Ltd.) are added respectively. Conduct high-temperature tests on the obtained low-sulfur marine fuel oil and the marine fuel oil in Example 1: After placing at 80 °C for 30 days, test the compatibility index, and the results are shown in Table 4 as follows:

[0084] Table 4

[0085]

[0086] Note: In Table 4, "Initial" refers to the compatibility index of the low-sulfur marine fuel oil before the high-temperature test.

[0087] Generally, when low-sulfur marine fuel oil is placed in a high-temperature environment for a long time, oxidation and polycondensation reactions are likely to occur, resulting in an increase in compatibility. If the compatibility of the low-sulfur marine fuel oil > 2 levels after being placed at high temperature for a period of time, it indicates that the high-temperature stability of the low-sulfur marine fuel oil is poor; on the contrary, if the compatibility of the low-sulfur marine fuel oil ≤ 2 levels after being placed at high temperature for a period of time, it indicates that the high-temperature stability of the low-sulfur marine fuel oil is good. It can be seen from Table 4 that the low-sulfur marine fuel oil provided in the present invention can remain stable at high temperature even without adding antioxidants. When a trace amount of antioxidant is added, the high-temperature stability of the low-sulfur marine fuel oil can be further improved, and the compatibility can be stabilized at level 1.

[0088] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solutions of the present invention, including any other suitable combination of each technical feature. These simple modifications and combinations should also be regarded as the content disclosed by the present invention and fall within the protection scope of the present invention.

Claims

1. A marine fuel oil, characterized in that, Based on the total amount of the marine fuel oil, the marine fuel oil comprises 10 - 50 wt% of base oil, 11 - 53 wt% of low-sulfur atmospheric and vacuum residue, 9 - 30 wt% of aromatic components, 10 - 50 wt% of low-sulfur distillate, and an antioxidant optionally; Wherein, the base oil is selected from the atmospheric tower bottom oil of the ebullated bed residue hydrotreating process and / or the middle section heavy wax oil of the vacuum tower of the ebullated bed residue hydrotreating process; the distillation range of the atmospheric tower bottom oil of the ebullated bed residue hydrotreating process is 356 - 482 °C; the distillation range of the middle section heavy wax oil of the vacuum tower of the ebullated bed residue hydrotreating process is 380 - 510 °C; The sulfur content of the low-sulfur atmospheric and vacuum residue is ≤ 1.5 wt%; The aromatic components are selected from at least one of catalytic slurry oil, catalytic recycle oil, and catalytic diesel oil. Among them, the final boiling point of the catalytic slurry oil is ≤ 480 °C; the distillation range of the catalytic recycle oil is 362 - 425 °C; the distillation range of the catalytic diesel oil is 224 - 313 °C; The sulfur content of the low-sulfur distillate is ≤ 0.5 wt%, and it is selected from at least one of residue plus wax oil, straight-run wax oil, V hydrofined wax oil, and hydro-upgrading heavy pyrolysis tar; the residue plus wax oil is a fraction with a distillation range of 330 - 450 °C taken from the atmospheric tower of the ebullated bed residue hydrotreating process; the V hydrofined wax oil is a fraction with a distillation range of 325 - 527 °C taken from the wax oil hydrofining unit; the hydro-upgrading heavy pyrolysis tar is a fraction with a distillation range of 250 - 380 °C taken from the ethylene pyrolysis tar hydrogenation unit; Among them, all the above distillation ranges refer to the temperature range from the 10% distillation temperature to the 90% distillation temperature; among them, the 10% distillation temperature and the 90% distillation temperature refer to the temperatures when the distillation volumes reach 10% and 90% of the sample respectively.

2. The marine fuel oil according to claim 1, wherein, Based on the total amount of the marine fuel oil, the marine fuel oil comprises 20 - 45 wt% of base oil, 11 - 25 wt% of low-sulfur atmospheric and vacuum residue, 15 - 25 wt% of aromatic components, and 25 - 45 wt% of low-sulfur distillate.

3. The marine fuel oil according to claim 1, wherein, The sulfur content of the atmospheric tower bottom oil of the ebullated bed residue hydrotreating process is 0.5 - 0.8 wt%.

4. The marine fuel oil according to claim 1, wherein The sulfur content of the middle section heavy wax oil of the vacuum tower of the ebullated bed residue hydrotreating process is 0.2 - 0.45 wt%.

5. The marine fuel oil according to claim 1, wherein The sulfur content of the low-sulfur atmospheric and vacuum residue is ≤ 1 wt%.

6. The marine fuel oil according to claim 1, wherein, The content of Si + Al after solid removal from the catalytic slurry oil is ≤ 200 ppm, the aromatic content is 90 - 95 wt%, the sulfur content is ≤ 0.6 wt%, and the kinematic viscosity at 50 °C is 220 - 240 mm² / s.

7. The marine fuel oil according to claim 1, wherein, The aromatic content of the catalytic recycle oil is 84 - 88 wt%, the sulfur content is ≤ 0.6 wt%, and the kinematic viscosity at 50 °C is 11 - 15 mm² / s.

8. The marine fuel oil according to claim 1, wherein, The aromatic content of the catalytic diesel oil is 80 - 85 wt%, the sulfur content is ≤ 0.4 wt%, and the kinematic viscosity at 50 °C is 2 - 3 mm² / s.

9. The marine fuel oil according to claim 1, wherein, The aromatic components are a mixture of catalytic slurry oil and / or catalytic recycle oil and catalytic diesel oil; among them, based on the total amount of the aromatic components, the content of catalytic diesel oil is 15 - 50 wt%.

10. The marine fuel oil according to claim 9, wherein, The aromatic hydrocarbon component is a mixture of catalytic slurry oil and / or catalytic recycled oil and catalytic diesel; wherein, based on the total amount of the aromatic hydrocarbon component, the content of catalytic diesel is 25-35 wt%.

11. The marine fuel oil according to claim 1, wherein, The sulfur content of the residue plus wax oil is 0.2-0.4 wt%.

12. The marine fuel oil according to claim 1, wherein, The straight-run wax oil is a fraction with a distillation range of 316-426 °C taken from the atmospheric and vacuum distillation column of crude oil; wherein, the sulfur content of the straight-run wax oil is 0.2-0.35 wt%. Among them, the distillation range refers to the temperature range from the 10% distillation temperature to the 90% distillation temperature; wherein, the 10% distillation temperature and the 90% distillation temperature refer to the temperatures when the distillation volumes reach 10% and 90% of the sample respectively.

13. The marine fuel oil according to claim 1, wherein, The sulfur content of the V hydrofined wax oil is 0.09-0.2 wt%.

14. The marine fuel oil according to claim 1, wherein, The sulfur content of the hydro-upgraded heavy cracking tar is 0.09-0.2 wt%, and the asphaltene content ≤ 5 wt%.

15. The marine fuel oil according to claim 1, wherein, The low-sulfur fraction is V hydrofined wax oil and / or hydro-upgraded heavy cracking tar.

16. The marine fuel oil according to claim 1, wherein, The marine fuel oil includes 110-280 ppm of an antioxidant, and the antioxidant is selected from 44PD.

17. The marine fuel oil according to claim 16, wherein, The marine fuel oil includes 120-180 ppm of an antioxidant.

18. The preparation method of the marine fuel oil according to any one of claims 1-17, characterized in that, The method includes: mixing a base oil, a low-sulfur atmospheric and vacuum residue, an aromatic hydrocarbon component, a low-sulfur fraction, and an optional antioxidant to obtain a marine fuel oil.

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