CN115786013A - Low-sulfur marine fuel oil and preparation method thereof - Google Patents
Low-sulfur marine fuel oil and preparation method thereof Download PDFInfo
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- CN115786013A CN115786013A CN202111065751.8A CN202111065751A CN115786013A CN 115786013 A CN115786013 A CN 115786013A CN 202111065751 A CN202111065751 A CN 202111065751A CN 115786013 A CN115786013 A CN 115786013A
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- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 147
- 239000011593 sulfur Substances 0.000 title claims abstract description 147
- 239000010762 marine fuel oil Substances 0.000 title claims abstract description 27
- 238000002360 preparation method Methods 0.000 title abstract description 13
- 239000003921 oil Substances 0.000 claims abstract description 170
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 77
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 44
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 36
- 238000009835 boiling Methods 0.000 claims abstract description 30
- 239000002893 slag Substances 0.000 claims abstract description 6
- 239000010747 number 6 fuel oil Substances 0.000 claims description 45
- 230000003197 catalytic effect Effects 0.000 claims description 30
- 238000002156 mixing Methods 0.000 claims description 27
- 238000003756 stirring Methods 0.000 claims description 18
- 239000003963 antioxidant agent Substances 0.000 claims description 14
- 230000003078 antioxidant effect Effects 0.000 claims description 14
- 239000002002 slurry Substances 0.000 claims description 14
- 239000002283 diesel fuel Substances 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 8
- 125000003118 aryl group Chemical group 0.000 claims description 5
- 239000005864 Sulphur Substances 0.000 claims description 3
- 230000032683 aging Effects 0.000 abstract description 19
- 239000013049 sediment Substances 0.000 abstract description 12
- 230000000052 comparative effect Effects 0.000 description 22
- 239000000203 mixture Substances 0.000 description 10
- 238000012360 testing method Methods 0.000 description 7
- 238000004523 catalytic cracking Methods 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 230000002195 synergetic effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002006 petroleum coke Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the technical field of low-sulfur marine fuel oil, and discloses low-sulfur marine fuel oil and a preparation method thereof, wherein the low-sulfur marine fuel oil comprises 20 parts by weight of unconverted oil of a boiling bed residual oil hydrogenation device, 3-30 parts by weight of aromatic hydrocarbon component, 5-35 parts by weight of atmospheric and vacuum residual oil and 10-55 parts by weight of low-sulfur fraction; wherein the low-sulfur fraction is selected from slag wax oil with the sulfur content of 0.1-0.3wt% and/or V hydrofined wax oil with the sulfur content of 0.02-0.12 wt%. According to the invention, the aromatic hydrocarbon component, the atmospheric and vacuum residue oil and the low-sulfur fraction are utilized to blend the unconverted oil of the boiling bed residue oil hydrogenation device, so that the unconverted oil of the boiling bed residue oil hydrogenation device can be changed into valuable, the high-quality low-sulfur marine fuel oil can be obtained, the requirements of the low-sulfur marine fuel oil on the total sediment (aging) index, the sulfur content index, the viscosity index and other full performance indexes can be met, and the application prospect is good.
Description
Technical Field
The invention relates to the technical field of low-sulfur marine fuel oil, in particular to low-sulfur marine fuel oil and a preparation method thereof.
Background
The ebullated-bed hydrogenation process refers to a process in which a residual oil feed is mixed with hydrogen and then enters from the bottom of a reactor, and catalyst particles in the reactor are in a boiling state by means of internal and external circulation. The ebullated bed hydrogenation process has the advantages of wide raw material adaptability and high residual oil conversion rate, but also has the problem of utilization of unconverted oil.
Typically a heavy residue (e.g., fixed bed residue hydrogenation bottoms, atmospheric vacuum bottoms) can be blended with light components to produce a low sulfur bunker fuel oil. If the unconverted oil of the boiling bed residual oil hydrogenation device can be prepared into the low-sulfur bunker fuel oil, the product value of the unconverted oil of the boiling bed residual oil hydrogenation device can be greatly improved, and the benefit maximization is realized as far as possible.
However, compared with the fixed bed residue hydrogenation bottom oil and the atmospheric and vacuum tower bottom oil, the unconverted oil of the boiling bed residue hydrogenation device contains the specific flocculent asphaltene, and the structure of the unconverted oil is in an intermediate state of oil and petroleum coke and is closer to the petroleum coke. The flocculent asphaltene is difficult to dissolve, and the influence on the performance of the unconverted oil is shown in the high index of total sediment (aging), and the fluctuation range of the index is between 0.6 and 2.4 weight percent. Therefore, the low-sulfur bunker fuel oil prepared by using the unconverted oil of the boiling bed residual oil hydrogenation device is generally difficult to meet the requirement of the low-sulfur bunker fuel oil on the total sediment content.
In addition, the stability of unconverted oil of the boiling bed residual oil hydrogenation device is relatively poor, and the kinematic viscosity at 50 ℃ is generally 1000mm 2 About/s and about 0.8wt% of sulfur, and it is difficult to obtain high-quality low-sulfur bunker fuel oil.
Therefore, it is highly desirable to provide a high quality low sulfur bunker fuel oil prepared using unconverted oil from an ebullated bed residuum hydrotreater.
Disclosure of Invention
The invention aims to solve the problem that high-quality low-sulfur marine fuel oil is difficult to obtain by using unconverted oil of a boiling bed residual oil hydrogenation device in the prior art, and provides low-sulfur marine fuel oil and a preparation method thereof.
In order to achieve the above objects, in one aspect, the present invention provides a low-sulfur bunker fuel oil comprising 20 parts by weight of an ebullated bed residue hydrotreater unconverted oil, 3 to 30 parts by weight of an aromatic hydrocarbon component, 5 to 35 parts by weight of an atmospheric and vacuum residue, 10 to 55 parts by weight of a low-sulfur fraction; wherein the low-sulfur fraction is selected from slag wax oil with the sulfur content of 0.1-0.3wt% and/or V hydrofined wax oil with the sulfur content of 0.02-0.12 wt%.
In a second aspect, the invention provides a method for preparing low-sulfur bunker fuel oil, wherein the method comprises the following steps: mixing unconverted oil of a boiling bed residual oil hydrogenation device and aromatic hydrocarbon components for the first time, then adding atmospheric and vacuum residual oil for the second time, then adding low-sulfur fraction for the third time, and optionally adding an antioxidant for the fourth time to obtain the low-sulfur marine fuel oil.
According to the invention, the aromatic hydrocarbon component, the atmospheric and vacuum residue, the low-sulfur fraction and the optional antioxidant are used for blending the unconverted oil of the boiling bed residue hydrogenation device, the unconverted oil of the boiling bed residue hydrogenation device can be changed into valuable, the high-quality low-sulfur marine fuel oil is obtained, the requirements of the low-sulfur marine fuel oil on the total sediment (aging) index, the sulfur content index, the viscosity index and other full performance indexes are met, and the application prospect is good.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For numerical ranges, each range between its endpoints and individual point values, and each individual point value can be combined with each other to give one or more new numerical ranges, and such numerical ranges should be construed as specifically disclosed herein.
The first aspect of the invention provides low-sulfur bunker fuel oil, wherein the low-sulfur bunker fuel oil comprises 20 parts by weight of boiling bed residue hydrogenation unit unconverted oil, 3-30 parts by weight of aromatic hydrocarbon components, 5-35 parts by weight of atmospheric and vacuum residue, and 10-55 parts by weight of low-sulfur fraction; wherein the low-sulfur fraction is selected from slag wax oil with the sulfur content of 0.1-0.3wt% and/or V hydrofined wax oil with the sulfur content of 0.02-0.12 wt%.
The inventor of the invention discovers that the aromatic hydrocarbon component and the atmospheric and vacuum residue oil act synergistically to dissolve flocculent asphaltene in unconverted oil of a boiling bed residue oil hydrogenation device and reduce the total sediment (aging) index of the unconverted oil of the boiling bed residue oil hydrogenation device to be below 0.08%, so that the total sediment (aging) index of the blended low-sulfur marine fuel oil can meet the quality requirement of the low-sulfur marine fuel oil.
The high-quality low-sulfur marine fuel oil not only needs to have qualified total sediment (aging) indexes, but also needs to meet sulfur content and viscosity indexes. The unconverted oil of the ebullated bed residual oil hydrogenation device after blending the aromatic hydrocarbon component and the atmospheric and vacuum residual oil still needs to be further adjusted in sulfur content and viscosity index. Theoretically, the low-sulfur fraction can be used for balancing the sulfur content index of the bunker fuel oil, but due to the particularity of the unconverted oil of the boiling bed residual oil hydrogenation unit, the compatibility of the low-sulfur fraction and the unconverted oil is poor, and the total deposit index is increased. The inventor of the invention discovers through research that when slag wax oil with the sulfur content of 0.2-0.3wt% and/or V hydrofined wax oil with the sulfur content of 0.09-0.12wt% are adopted for blending, the total sediment index, the sulfur content and the viscosity index can be considered, and the high-quality low-sulfur marine fuel oil can be obtained.
In the invention, the residue and wax oil refers to a wax oil fraction which is extracted from an atmospheric tower in an ebullated bed residual oil hydrogenation process and is less than or equal to 540 ℃, and the V hydrofined wax oil refers to a fraction which is extracted from a wax oil hydrofining device and has a distillation cut point of 300-520 ℃.
In a preferred embodiment, the low sulfur bunker fuel oil comprises 20 parts by weight of ebullated bed residue hydrotreater unconverted oil, 5 to 20 parts by weight of aromatic hydrocarbon component, 6 to 25 parts by weight of atmospheric and vacuum residue, and 20 to 45 parts by weight of low sulfur fraction.
In a further preferred embodiment, the low sulfur bunker fuel oil comprises 20 parts by weight of ebullated bed residue hydrotreater unconverted oil, 10 to 15 parts by weight of aromatic hydrocarbon component, 20 to 25 parts by weight of atmospheric and vacuum residue, and 30 to 35 parts by weight of low sulfur fraction.
In a preferred embodiment, the unconverted oil of the boiling bed residual oil hydrogenation unit is from the bottom of a boiling bed residual oil hydrogenation vacuum tower and is a fraction with a distillation point being more than or equal to 450 ℃.
In a preferred embodiment, the aromatic content of the aromatic component is ≥ 20wt%, preferably 60-95wt%; a sulphur content of < 1.8 wt.%, preferably < 0.8 wt.%; the kinematic viscosity at 50 ℃ is less than or equal to 350mm 2 S, preferably 270mm or less 2 /s。
In a preferred embodiment, the aromatic hydrocarbon component is selected from one or more of catalytic oil slurry, catalytic diesel, catalytic medium oil, heavy aromatics, preferably catalytic oil slurry and/or catalytic diesel.
In the invention, catalytic oil slurry, catalytic diesel oil and catalytic first-middle oil are all from a catalytic cracking device, wherein residual oil discharged from the bottom of the catalytic cracking device is the catalytic oil slurry, the catalytic diesel oil is a fraction which is processed by the catalytic cracking device and then fractionated, the distillation range of the fraction is 180-350 ℃, the catalytic first-middle oil is from the middle part of a catalytic cracking fractionating tower, and heavy aromatics are from the bottom of an aromatic disproportionation device.
In a preferred embodiment, the Si + Al content of the catalytic slurry oil after being subjected to solid removal is less than or equal to 200ppm, the aromatic hydrocarbon content is 90-95wt%, the sulfur content is less than or equal to 0.65wt%, and the kinematic viscosity at 50 ℃ is 220-290mm 2 S; the content of the catalytic diesel oil aromatic hydrocarbon is 80-85wt%; sulfur content less than or equal to 0.4wt%, and kinematic viscosity at 50 ℃ of 2-3mm 2 And s. Wherein ppm in the present invention refers to mass unless otherwise specified.
In a preferred embodiment, the aromatic hydrocarbon component is catalytic slurry oil and catalytic diesel oil, wherein the mass ratio of the catalytic slurry oil to the catalytic diesel oil is from 2 to 7.
In a preferred embodiment, the aromatic hydrocarbon component is a catalytic slurry oil, and the mass percent of the catalytic slurry oil is less than or equal to 30%, preferably 20-30%, based on the total mass of the unconverted oil, the aromatic hydrocarbon component, the atmospheric and vacuum residue and the low-sulfur fraction of the ebullated bed residue hydrogenation unit.
In a preferred embodiment, the sulfur content of the atmospheric and vacuum residue is less than or equal to 1.5wt%, preferably less than or equal to 0.7wt%.
In a preferred embodiment, the low sulfur fraction is selected from the group consisting of a residue plus wax oil having a sulfur content of 0.2 to 0.3wt% and/or a V hydrofined wax oil having a sulfur content of 0.09 to 0.12 wt%.
In a further preferred embodiment, the low sulfur fraction is preferably a V hydrofined wax oil with a sulfur content of 0.09 to 0.12 wt.%.
The inventor finds that the V hydrofined wax oil with the sulfur content of 0.09-0.12wt% has better compatibility with unconverted oil of a boiling bed residual oil hydrogenation device and better effect of reducing the sulfur content index through research.
In a preferred embodiment, the low sulfur bunker fuel oil further comprises 50 to 150ppm, preferably 50 to 120ppm, of an antioxidant, wherein the antioxidant is selected from 44PD or T502A (2,6-di-tert-butyl mixed phenol).
In the invention, the addition of trace antioxidant can further improve the high-temperature stability of the low-sulfur marine fuel oil. 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.
In a second aspect, the present invention provides a method for preparing a low-sulfur bunker fuel oil according to the first aspect, wherein the method comprises: mixing unconverted oil of a boiling bed residual oil hydrogenation device and aromatic hydrocarbon components for the first time, then adding atmospheric and vacuum residual oil for the second time, then adding low-sulfur fraction for the third time, and optionally adding an antioxidant for the fourth time to obtain the low-sulfur marine fuel oil.
The high-quality low-sulfur marine fuel oil which gives consideration to the total sediment (aging) index, the sulfur content index and the viscosity index and meets the requirement of the low-sulfur marine fuel full-performance index can be prepared by controlling the mixing sequence of unconverted oil, aromatic hydrocarbon components, atmospheric and vacuum residue and low-sulfur fraction of the boiling bed residue hydrogenation device.
In a preferred embodiment, the first mixing is carried out at 40-60 ℃ and 80-120r/min with stirring for 5-15min.
In a preferred embodiment, the second mixing is performed at 70-90 deg.C under stirring at 80-120r/min for 10-20min, and then the stirring is stopped and the mixture is allowed to stand for 5-15min.
In a preferred embodiment, the third mixing is carried out at a temperature of 70-90 ℃ and a speed of 160-200r/min for 10-20min.
In a preferred embodiment, the fourth mixing is carried out at a temperature of 70-90 ℃ and a speed of 160-200r/min for a period of 10-20min.
The present invention will be described in detail below by way of examples. Among them, the boiling bed residue hydrogenation apparatus used in the examples and comparative examples had a total deposit (aged) of unconverted oil of 1.3wt%, a sulfur content of 0.8wt%, and a kinematic viscosity of 1000mm at 50 ℃ 2 /s；
The Si and Al content after the catalytic slurry oil is subjected to solid removal is 150ppm, the aromatic hydrocarbon content is 93wt%, the sulfur content is 0.6wt%, and the kinematic viscosity at 50 ℃ is 260mm 2 S; the catalytic diesel oil has aromatic hydrocarbon content of 82wt%, sulfur content of 0.4wt% and 50 deg.c kinematic viscosity of 2.5mm 2 /s；
The sulfur content of the atmospheric and vacuum residue is 0.7wt%; v the sulfur content of hydrorefined wax oil is 0.12wt%, and the sulfur content of slag wax oil is 0.21wt%.
Example 1
Placing unconverted oil of a boiling bed residual oil hydrogenation device in a preparation storage tank, heating the temperature of the preparation storage tank to 50 ℃, then adding an aromatic hydrocarbon component for first mixing, and stirring for 10min at a stirring speed of 100 r/min;
raising the temperature of a preparation storage tank to 80 ℃, adding atmospheric and vacuum residue oil for secondary mixing, stirring for 15min at a stirring speed of 100r/min, stopping stirring, and standing for 10min to complete dissolving of total sediments in unconverted oil of the boiling bed residue oil hydrogenation device;
and adding the low-sulfur fraction into a preparation storage tank for mixing for the third time, and stirring at the stirring speed of 180r/min at 80 ℃ for 10min to obtain the low-sulfur marine fuel oil.
Wherein, the consumption of unconverted oil, aromatic hydrocarbon components, atmospheric and vacuum residuum and low sulfur fraction of the boiling bed residuum hydrogenation unit and the properties of the obtained low sulfur bunker fuel oil are shown in table 1.
Examples 2 to 6
The same procedure as in example 1 was conducted except that the amounts of unconverted oil, aromatic hydrocarbon components, atmospheric and vacuum residue, low sulfur fraction used in the ebullated-bed residue hydrotreater and the properties of the resulting low-sulfur bunker fuel oil were as shown in Table 1.
Example 7
The preparation method is the same as that of the example 1, except that after the third mixing is completed, the antioxidant is added into a preparation storage tank for fourth mixing, and the mixture is stirred for 10min at the stirring speed of 180r/min at the temperature of 80 ℃ to obtain a series of low-sulfur bunker fuel oil. Wherein, the obtained low-sulfur bunker fuel oil antioxidant and the content thereof are shown in table 2.
A series of low sulfur bunker fuel oils prepared in example 1 and example 7 were subjected to high temperature testing: after 30 days at 80 ℃, the total deposit (aging) index was measured and the results are shown in table 2.
TABLE 2
Note: table 2 initially refers to the total deposit (aging) indicator for low sulfur bunker fuel oil before high temperature testing.
As can be seen from table 2, the addition of the antioxidant can prevent the formation of deposits, and contributes to the improvement of the stability of the low-sulfur bunker fuel oil in a high-temperature environment.
Comparative example 1
The same as in example 4, except that atmospheric and vacuum residue was not added, the composition and properties of the obtained low-sulfur bunker fuel oil are shown in table 1.
Comparative example 2
The same as in example 4, except that no aromatic hydrocarbon component was added, the composition and properties of the obtained low-sulfur bunker fuel oil are shown in table 1.
As can be seen from the results of comparative example 4 and comparative examples 1 and 2, the use of either the aromatic hydrocarbon component or the atmospheric and vacuum residue alone under the same conditions did not result in a low sulfur bunker fuel oil having a total deposit (aging) index meeting the requirements. The synergistic effect of the aromatic hydrocarbon component and the atmospheric and vacuum residue can not only reduce the total sediment (aging) index of unconverted oil at the bottom of the boiling bed residue hydrogenation vacuum tower, but also can blend the kinematic viscosity at 50 ℃ to meet the index requirement of low-sulfur marine fuel oil products.
Comparative example 3
The same as example 4, except that the amount of the atmospheric and vacuum residue was 4g, the composition and properties of the resulting low-sulfur bunker fuel oil were as shown in table 1.
It can be seen from comparative example 4 and comparative example 3 that when the amount of the atmospheric and vacuum residue is small, the synergistic effect of the aromatic hydrocarbon component and the atmospheric and vacuum residue is weak, and it is difficult to obtain a low-sulfur bunker fuel oil having a total deposit (aging) index satisfying the requirements.
Comparative example 4
The same as in example 5, except that the amount of the aromatic hydrocarbon component added was 6g, the composition and properties of the obtained low-sulfur bunker fuel oil were as shown in Table 1.
It can be seen from comparative example 5 and comparative example 4 that when the amount of the aromatic hydrocarbon component is relatively small, the synergistic effect of the aromatic hydrocarbon component and the atmospheric and vacuum residue is relatively weak, and it is difficult to obtain a low-sulfur bunker fuel oil having a total deposit (aging) index meeting the requirement.
Comparative example 5
The composition and properties of the low sulfur bunker fuel oil obtained in the same manner as in example 4, except that the atmospheric and vacuum residue was replaced with equal mass of DAO (deasphalted oil from solvent deasphalting, sulfur content 0.75 wt%), are shown in table 1.
From the test results of comparative example 5, it is known that although the unconverted oil of the ebullated bed residue hydrotreater can be blended by using DAO so that the kinematic viscosity at 50 ℃ and the sulfur content meet the requirements of the low-sulfur marine fuel, the blended low-sulfur marine fuel has high total deposit (aging) index, and the qualified low-sulfur marine fuel cannot be obtained.
Comparative example 6
The same as in example 2, except that an equal mass of heavy pyrolysis tar (0.12% by weight in terms of sulfur content, 5%) was usedKinematic viscosity at 0 ℃ of 100mm 2 /s) replace V hydrofined wax oil, and the composition and the properties of the obtained low-sulfur marine fuel oil are shown in Table 1.
From the test results of comparative example 6, it is demonstrated that the low sulfur fraction heavy cracked tar, although the index of sulfur content can be adjusted, has poor compatibility with unconverted oil at the bottom of the ebullated bed vacuum column, and the index of total sediment (aging) after adjustment is obviously poor.
Comparative example 7
79g of a hydrogenation clinker fraction (sulfur content 0.42wt%, kinematic viscosity at 50 ℃ 270 mm) of a fixed bed residue hydrotreater 2 /s) placing the mixture in a preparation storage tank, heating the preparation storage tank to 50 ℃, then adding 11g of catalytic oil slurry and 10g of catalytic diesel oil, mixing, and stirring for 10min at a stirring speed of 100 r/min; obtaining low-sulfur bunker fuel oil; wherein the obtained low-sulfur marine fuel oil has the total deposit (aging) index of 0.01 percent, the sulfur content of 0.38 weight percent and the kinematic viscosity at 50 ℃ of 167mm 2 /s。
Comparative example 8
The same as in comparative example 7, except that: and replacing the bottom oil of the fixed bed residual oil hydrogenation tower with unconverted oil of the boiling bed residual oil hydrogenation device. Wherein the obtained bunker fuel oil has the total deposit (aging) index of 1.02wt%, the sulfur content of 0.5% and the kinematic viscosity at 50 ℃ of 230mm 2 /s。
From the test results of comparative example 7 and comparative example 8, it can be seen that although both the fixed bed residue hydrogenation bottom oil and the unconverted oil of the ebullated bed residue hydrogenation apparatus are heavy residues, the conventional blending method for heavy residues is not suitable for the unconverted oil of the ebullated bed residue hydrogenation apparatus because the unconverted oil of the ebullated bed residue hydrogenation apparatus contains specific flocculent asphaltenes.
Comparative example 9
The same as example 1, except that the order of addition of the atmospheric and vacuum residue and the low sulfur fraction was changed, that is, the atmospheric and vacuum residue was used in place of the low sulfur fraction in the second mixing, and the low sulfur fraction was used in place of the atmospheric and vacuum residue in the third mixing, the properties of the resulting low sulfur bunker fuel oil were as shown in table 1.
It can be known from the comparison between example 1 and comparative example 9 that the blending sequence of the unconverted oil, the aromatic hydrocarbon component, the atmospheric and vacuum residue and the low-sulfur fraction of the residue hydrogenation unit in the ebullated bed has a certain influence on the blending of the total deposit (aging) index, and when the blending is performed according to the blending sequence of the unconverted oil, the aromatic hydrocarbon component, the atmospheric and vacuum residue and the low-sulfur fraction of the residue hydrogenation unit in the ebullated bed, the high-quality low-sulfur bunker fuel oil which gives consideration to the total deposit (aging) index, the sulfur content index and the viscosity index can be prepared.
TABLE 1
Note: the test recipe for the total deposit (aged) in Table 1 was SH/T0702, the test method for the sulfur content was GB/T17040, and the test method for the viscosity was GB/T11137.
Test example 1
The low sulfur bunker fuel prepared in example 1 was tested for overall performance and the results are shown in table 3:
TABLE 3
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. The low-sulfur bunker fuel oil is characterized by comprising 20 parts by weight of boiling bed residue hydrogenation unit unconverted oil, 3-30 parts by weight of aromatic hydrocarbon components, 5-35 parts by weight of atmospheric and vacuum residue and 10-55 parts by weight of low-sulfur fraction; wherein the low-sulfur fraction is selected from slag wax oil with the sulfur content of 0.1-0.3wt% and/or V hydrofined wax oil with the sulfur content of 0.02-0.12 wt%.
2. The low sulfur bunker fuel oil of claim 1, wherein the aromatic content of the aromatic component is not less than 20wt%, preferably 60-95wt%; a sulphur content of < 1.8 wt.%, preferably < 0.8 wt.%; kinematic viscosity at 50 ℃ is less than or equal to 350mm 2 S, preferably 270 wt.% or less;
preferably, the aromatic hydrocarbon component is selected from one or more of catalytic oil slurry, catalytic diesel, catalytic medium oil, heavy aromatics.
3. The low sulfur bunker fuel oil according to claim 2, wherein the aromatic hydrocarbon component is catalytic slurry oil and catalytic diesel oil, and the mass ratio of the catalytic slurry oil to the catalytic diesel oil is 2-7.
4. The low sulfur bunker fuel oil of claim 1, wherein the sulfur content of the atmospheric and vacuum residue is less than or equal to 1.5wt%, preferably less than or equal to 0.7wt%.
5. The low sulfur bunker fuel oil of claim 1, wherein the low sulfur fraction is a V hydrofined wax oil having a sulfur content of 0.09% to 0.12 wt%.
6. The low sulphur bunker fuel oil of claim 1, further comprising 50-150ppm, preferably 50-120ppm, of an antioxidant selected from 44PD and/or T502A.
7. The low sulfur bunker fuel oil of claim 6 wherein the antioxidant is 44PD.
8. A method for preparing low sulfur bunker fuel oil, comprising:
mixing unconverted oil of a boiling bed residual oil hydrogenation device and aromatic hydrocarbon components for the first time, then adding atmospheric and vacuum residual oil for the second time, then adding low-sulfur fraction for the third time, and optionally adding an antioxidant for the fourth time to obtain the low-sulfur marine fuel oil.
9. The low sulfur bunker fuel oil of claim 8, wherein the first mixing is performed at 40-60 ℃ and 80-120r/min with stirring for 5-15min; and stirring for 10-20min at 70-90 ℃ and 80-120r/min for the second time, stopping stirring, and standing for 5-15min.
10. The low sulfur bunker fuel oil of claim 8, wherein the third mixing is performed at a temperature of 70-90 ℃ and a stirring speed of 160-200r/min for 10-20min; the fourth mixing is carried out at 70-90 ℃ and at 160-200r/min for 10-20min under stirring.
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| CN103642539A (en) * | 2013-12-25 | 2014-03-19 | 济南开发区星火科学技术研究院 | Regulating method of bunker fuel oil |
| JP2020105292A (en) * | 2018-12-26 | 2020-07-09 | 出光興産株式会社 | Fuel oil composition for internal combustion engine |
| CN110205160A (en) * | 2019-06-11 | 2019-09-06 | 黄河三角洲京博化工研究院有限公司 | It is taken off based on catalytic cracked oil pulp and consolidates-add the process that hydrogen prepares bunker fuel oil |
| CN113322107A (en) * | 2020-08-26 | 2021-08-31 | 中国石油天然气股份有限公司 | Marine residual fuel oil and preparation method thereof |
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