KR20210039743A - A Very Low Sulfur Fuel Oil and a method for producing the same - Google Patents

Abstract

The present invention provides a production method of ultra low sulfur fuel oil capable of producing high-quality ultra low sulfur fuel oil having high stability, and ultra low sulfur fuel oil produced by the production method. The production method of ultra low sulfur fuel oil having high compatibility and high stability comprises the steps of: mixing petroleum residua obtained from at least two different petroleum refining processes, adding a hydrocarbon solvent to the residual petroleum mixture, heating the mixture of the petroleum residua mixture and hydrocarbon solvent to extract and recover a mixture of oil fractions and the hydrocarbon solvent from the mixture of the petroleum residua mixture and hydrocarbon solvent with raffinate having asphaltenes therein being left, and removing the hydrocarbon solvent from the mixture of the oil fractions and the hydrocarbon solvent, thereby obtaining ultra low sulfur fuel oil, wherein the ultra low sulfur fuel oil has a sulfur content of 0.5 wt% or less based on the total weight of the ultra low sulfur fuel oil, and ultra low sulfur fuel oil produced by the production method.

Description

A Very Low Sulfur Fuel Oil and a Method for Producing the Same}

In the present invention, in the production of ultra-low sulfur fuel oil, a hydrocarbon solvent having 3, 4 or 5 carbon atoms is added and heated to an oil mixture obtained by mixing at least two types of oil remaining after producing high quality oil in a petroleum refining process, Prepared by recovering a mixture of oil and hydrocarbon solvent from the oil mixture, removing asphaltene by remaining in the raffinate, removing hydrocarbon solvent from the mixture of oil and hydrocarbon solvent, and not more than 0.5% by weight based on the total weight. The present invention relates to a method for producing ultra-low sulfur fuel oil having a sulfur content and to the ultra-low sulfur fuel oil, in particular, ship oil.

With the application of the regulation on the sulfur content of ship oil by the International Marine Organization (IMO) from 2020, the refinery industry has entered a new phase in the production of ship oil. As the sulfur content regulation standard of ship oil has been greatly strengthened from less than 3.5% by weight of existing sulfur to less than 0.5% by weight, additional desulfurization process treatment of existing ship oil products has become essential.

In the existing literature, low asphaltene content and high aromatic compound content are suggested as criteria for securing oil stability.In order to balance the content between components, oils with different production processes are mixed (e.g., primary refined fuel oil). (Straight-run fuel oil and cracked oil), when oils with a large difference in viscosity and density are mixed (e.g. FCC Slurry Oil: Fluidized Catalytic Cracker Slurry Oil) and diesel It is known that the incompatibiliy of the mixed oil is increased due to the combination of oil) and asphaltene agglomeration. In the oil containing a large amount of saturated hydrocarbon compounds and asphaltenes, due to relatively few aromatic compounds, asphaltenes in the oil are not completely dispersed in the form of micelles, and aggregation and precipitation occur over time. It is judged that the oil produced by a single process that behaves as above over time has low stability. Even if the oil has sufficient stability in its individual state, the tendency to generate impurities such as sludge and sediment may accelerate as it is mixed with other oils derived from other processes of crude oil refining, and in this case, it is judged that compatibility is insufficient.

As such, as the sulfur content regulations have been greatly strengthened, it has become difficult to produce products with price competitiveness with oil produced in a single process, such as existing marine oil, and most of the products blend ultra-low sulfur oil with the existing high sulfur oil. You can think of production in a way. In addition, as the profitability of the refinery process continues to deteriorate, many refiners have high acidity and contain excessive amounts of impurities such as sulfur, nitrogen, and metals, but operate in the direction of increasing the input amount of low-quality crude oil. There is concern about deterioration of the quality of ship oil using private oil as a raw material. Accordingly, in order to satisfy the sulfur content standard of 0.5% by weight or less, the ratio of the ultra-low sulfur oil, which was mixed in trace amounts, must be rapidly increased, and in some cases, mixing of different residual oils produced through two or more production processes is attempted. It could be. These attempts can have a serious impact on the stability of the oils mentioned above.

Many analysis methods have been suggested as a method of measuring the stability and miscibility of oil (i.e., stability and compatibility), and one of the methods that can be intuitively judged is the Spot Test (ASTM D4740), and its criteria are It is shown in 1, and the criterion for determining the spot test is called the Spot Rating, and the rating can be classified into 1 to 5.

Even if the oil containing a lot of saturated and asphaltenes is a single oil, the spot rating may deteriorate with the increase of solids and sludge due to agglomeration of asphaltenes over time. Mixed oils due to the blending of oils from different production processes can immediately observe the change in the spot rating compared to the case of single oil, and the oil is very unstable in the case of a spot rating of 3 or higher, further deteriorating stability during long-term storage at the ship's fluency. Is inevitable, and in this case, it will seriously affect the normal operation of the purifier and engine in the ship's fuel system. Stable production of marine oil using residual oil as a raw material can be achieved through the additional treatment of a limited process (VRDS: Vacuum Residue Desulfurization) in the manufacturing facility, which is very advanced and has an excessive operating cost (due to excessive hydrogen use), but this is profitable. It is not possible to secure oil from various upper processes as raw materials, so it is possible to produce only a limited amount of oil. If the vast amount of high-sulfur ship oil that has been used in all high seas has to be replaced with ultra-low sulfur fuel oil, if it is produced only through a limited process, it is difficult to meet sufficient demand and face an unfavorable environment in terms of cost competitiveness.

In the present invention, in order to overcome the problems caused by mixing different types of oils as described above and the disadvantages of the conventional technology, the manufacturing process is relatively simple, so that a large amount of investment is not required. Raw materials, especially oils remaining after producing high-quality oil, can be utilized, and manufacturing costs can also be drastically reduced, that is, oils that can be used in the production of ship oil produced in the refinery process and mixed with a predetermined blending ratio. The purpose is to provide VLSFO with high stability (Spot Rating 1) using an oily mixture as a raw material.

The manufacturing method of ultra-low sulfur fuel oil according to the present invention comprises: (1) a mixing step of producing a high-quality oil in a petroleum refining process and mixing the remaining at least two types of oil to obtain an oil mixture; (2) An asphaltene separation step of adding and heating a hydrocarbon solvent having 3, 4 or 5 carbon atoms to the oil mixture to recover a mixture of oil and hydrocarbon solvent from the oil mixture, and to remove asphaltene by remaining in the raffinate. ; And (3) a refining step of removing the hydrocarbon solvent from the mixture of the oil component and the hydrocarbon solvent to obtain an ultra-low sulfur fuel oil, and having a sulfur content of 0.5% by weight or less based on the total weight. Get

The oil used in the mixing step is AR (Atmospheric Residue; atmospheric pressure residual oil), VR (Vacuum Residue; decompression residual oil), t-AR (hydrotreated Atmospheric Residue; desulfurization atmospheric pressure residual oil), t-VR (hydrotreated Vacuum Residue; Desulfurization and reduced pressure residue), DAO (Deasphalted Oil; deasphalted oil), t-DAO (hydrotreated Deasphalted Oil; desulfurized and deasphalted oil), UCO (Unconverted Oil; unconverted oil (or HCR process residue), VGO (Vacuum Gas Oil) ; Decompression gas oil), t-VGO (hydrotreated VGO, desulfurization decompression gas oil), HSD (High sulfur Diesel; high sulfur diesel oil), ULSD (Ultra Low Sulfur Diesel; ultra low sulfur diesel oil) can be selected from the group consisting of). .

The hydrocarbon solvent having 3, 4 or 5 carbon atoms used in the asphaltene separation step is preferably from the group consisting of n-propane, n-butane, i-butane, n-pentane, i-pentane, and mixtures of two or more thereof. It is selected, more preferably selected from the group consisting of n-pentane, i-pentane, and mixtures thereof, and most preferably n-pentane.

In the asphaltene separation step, a hydrocarbon solvent having 3, 4 or 5 carbon atoms at a pressure in the range of 30 to 50 barg (instrument pressure) and a temperature in the range of 100 to 230°C is used in an amount of 1 to 4 times the volume of the oil mixture. The asphaltene is separated by addition (hydrocarbon solvent: oil mixture = 1 to 4: 1), and the mixed oil is separated and recovered to reduce the mixed oil, that is, the asphaltene content in the prepared ultra-low sulfur fuel oil.

The ultra-low sulfur fuel oil according to the present invention is produced by producing high-quality oil in a petroleum refining process and adding a hydrocarbon solvent having 3, 4 or 5 carbon atoms to an oil mixture obtained by mixing at least two of the remaining oils and heating the oil. Obtained by recovering a mixture of oil and hydrocarbon solvent from the mixture, removing asphaltene by remaining in the raffinate, and removing the hydrocarbon solvent from the mixture of oil and hydrocarbon solvent, the sulfur content of which is 0.5% by weight or less based on the total weight The ultra-low sulfur fuel oil of the present invention is preferably within the range of 0.1 to 0.6% by weight, more preferably within the range of 0.05 to 0.55% by weight, and most preferably within the range of 0.01 to 0.50% by weight based on the total weight. It may have an asphaltene content of.

According to the present invention, it is possible to produce high-quality oil in various processes of petroleum refining, and to produce high-quality ultra-low sulfur fuel oil with high stability by using various oils remaining as raw materials. It can be selected, and limited raw materials such as hydrodesulfurization are used, and production and manufacturing costs can be drastically reduced compared to an advanced process that requires high operating costs.

This effect is that the very low sulfur fuel oil (VLSFO) produced by the present invention shows a difference in behavior and stability from the existing marine oil when it is put into a purifier and engine in a ship, which is indispensable to oil. It is analyzed to be due to changes in components (mainly, saturates, aromatics, resins, and asphaltenes) contained in the oil.

1 is a photograph showing the Spot Rating of the Spot Test (ASTM D4740) for evaluating the stability of fuel oil.
FIG. 2 is a schematic diagram illustrating a process of preparing ultra-low sulfur fuel oil by separating and removing asphaltene from an oil mixture according to the present invention.

The manufacturing method of ultra-low sulfur fuel oil according to the present invention comprises: (1) a mixing step of producing a high-quality oil in a petroleum refining process and mixing the remaining at least two types of oil to obtain an oil mixture; (2) A hydrocarbon solvent having 3, 4 or 5 carbon atoms is added to the oil mixture and heated to extract and separate asphaltene from the oil mixture and remain with raffinate, and the oil component is volatilized with a hydrocarbon solvent to separate oil and hydrocarbons. An asphaltene separation step of recovering as a mixture of solvents; And (3) a refining step of removing the hydrocarbon solvent from the mixture of the oil component and the hydrocarbon solvent to obtain an ultra-low sulfur fuel oil; and an ultra-low sulfur fuel having a sulfur content of 0.5% by weight or less based on the total weight. Oil is provided, and the oil used in the mixing step is AR (Atmospheric Residue), VR (Vacuum Residue), t-AR (hydrotreated Atmospheric Residue; desulfurization atmospheric residual oil), t-VR (hydrotreated Vacuum Residue; desulfurized vacuum residue), DAO (Deasphalted Oil; deasphalted oil), t-DAO (hydrotreated Deasphalted Oil; desulfurized and deasphalted oil), UCO (Unconverted Oil; unconverted oil (or HCR process residue), Group consisting of VGO (Vacuum Gas Oil), t-VGO (hydrotreated VGO, desulfurized decompression gas oil), HSD (High sulfur Diesel), ULSD (Ultra Low Sulfur Diesel). Can be selected from

In this specification, “high-quality oil” refers to oil having a low boiling point and high economic value, such as jet fuel and gasoline, and the “oil remaining after producing high-quality oil” to which the present invention is applied refers to the sulfur content or ash. It has a high palten content and refers to oils mainly obtained as a by-product in the form of residual oil.

That is, in the present invention, a hydrocarbon solvent having 3, 4 or 5 carbon atoms, preferably n-propane, n-butane, i-butane, n-pentane, i- A hydrocarbon solvent selected from the group consisting of pentane and a mixture of two or more thereof, more preferably n-pentane or i-pentane, most preferably n-pentane, is added as a source material causing aggregation and precipitation from mixed oil. By separating asphaltene, ultra-low sulfur fuel oil can be produced.

For the separation of asphaltene, the ratio of the hydrocarbon solvent having 3, 4 or 5 carbon atoms and the mixed oil (hydrocarbon solvent: oil mixture) is 1 to 4: 1, more preferably 2 to 3: 1 by volume, and the pressure is 30 to 50 barg, more preferably 35 to 46 barg, most preferably 38 to 43 barg, and the temperature is -20 to +20°C, more preferably -15, based on the critical temperature of the hydrocarbon solvent used. To +15°C, most preferably -10 to +10°C, which may be a temperature in the range of 100 to 230°C.

After separation of asphaltene, the hydrocarbon solvent is removed from the recovered fraction and the hydrocarbon solvent mixture to obtain ultra-low sulfur fuel oil, the recovered hydrocarbon solvent can be reused, and the raffinate stream is used as a blended fraction to increase the fluidity of the coke raw material. Can be.

The inventors of the present invention have shown a strong solvent effect as the carbon number of the hydrocarbon solvent increases through repeated experiments. However, the efficiency of removing asphaltene from the mixed oil when a hydrocarbon solvent having a high solvent effect such as hexane having 6 carbon atoms is used. This greatly decreased, and it was confirmed that even in the case of the same carbon number, a linear hydrocarbon (eg, n-pentane) exhibited a strong solvent effect compared to a branched hydrocarbon (eg, i-pentane). In addition, it was confirmed that the yield increased at low temperature and high pressure according to the density change and thermodynamic preference of the hydrocarbon solvent in the supercritical state in the extraction column in which the extraction was performed in the asphaltene separation step. The present inventors confirmed that an appropriate hydrocarbon solvent should be used to prevent oil loss and secure the maximum yield of VLSFO with improved stability. In particular, it was necessary to select an appropriate hydrocarbon solvent to increase the stability of the oil mixture. I could confirm.

The ultra-low sulfur fuel oil of the present invention from which asphaltene is separated has a sulfur content within the range of 0.001 to 0.5% by weight, preferably 0.05 to 0.49% by weight, and most preferably 0.1 to 0.48% by weight, based on the total weight. I can.

The ultra-low sulfur fuel oil according to the present invention exhibits improved aging stability despite manufacturing high-quality oil in petroleum refining processes and mixing the remaining oils.

That is, the oil generated during petroleum refining has a high saturation content or a high content of asphaltene, and thus its stability is low when a fuel oil is manufactured using it as a raw material. However, the present invention relates to an AR (Atmospheric Residue); Reason), VR (Vacuum Residue; Deasphalted Residue), t-AR (hydrotreated Atmospheric Residue; Desulfurized Atmospheric Residue), t-VR (hydrotreated Vacuum Residue; Desulfurized Decompression Residue), DAO (Deasphalted Oil; deasphalted oil) , t-DAO (hydrotreated Deasphalted Oil), UCO (Unconverted Oil; unconverted oil (or HCR process residue), VGO (Vacuum Gas Oil), t-VGO (hydrotreated VGO, desulfurization decompression) Gas oil), HSD (High sulfur Diesel; High sulfur diesel oil), ULSD (Ultra Low Sulfur Diesel; Ultra Low Sulfur Diesel), a mixture of two or more oils in a predetermined component ratio is treated with a hydrocarbon solvent to remove asphaltene. It is characterized by providing ultra-low sulfur fuel oil having high stability by reducing the asphaltene content in mixed oil while satisfying the sulfur content regulation of ultra-low sulfur fuel oil.

Hereinafter, the manufacturing method of the present invention will be described in detail by examples.

[Example 1]

t-AR: 1,457,000ℓ of an oily mixture of t-DAO in a volume ratio of 1:1 was added at 42 barg and n-pentane as a solvent at 205℃ in a ratio of 2 by volume ratio of the solvent/oil mixture for 60 minutes (extraction column Residence time) during extraction treatment (total operation time of the extraction process: 660 minutes) to remove asphaltene to remain in the raffinate, and recover the oil and solvent mixture by volatilization, and then separate the solvent from the recovered oil and solvent mixture. 1,394,000 liters of low sulfur fuel oil were obtained. The sulfur content, asphaltene content, yield, spot rating by the spot test immediately after removal of asphaltene, and the spot rating with time change by the spot test were measured in the obtained ultra-low sulfur fuel oil, and these results are shown in Table 1. Sulfur content analysis was measured by ASTM D4294, asphaltene content analysis was measured by ASTM D6560.

[Example 2]

t-AR: 1,643,000ℓ of an oily mixture of t-DAO in a volume ratio of 1: 1 was added at 42 barg and n-pentane as a solvent at 185℃ in a ratio of 2 by volume ratio of the solvent/oil mixture for 40 minutes (extraction column Residence time) during extraction treatment (total operation time of the extraction process: 480 minutes) to remove asphaltene to remain in the raffinate, and recover the oil and solvent mixture by volatilization, and then separate the solvent from the recovered oil and solvent mixture. 1,615,000 liters of low sulfur fuel oil were obtained. The sulfur content, asphaltene content, yield, spot rating by the spot test immediately after removal of asphaltene, and the spot rating with time change by the spot test were measured in the obtained ultra-low sulfur fuel oil, and these results are shown in Table 1.

[Example 3]

t-AR: 1,325,000ℓ of an oily mixture of t-DAO in a volume ratio of 1: 1 was added as a solvent under the condition of 42 barg and 220℃, and i-pentane was added in a ratio of 1 to the volume ratio of the solvent/oil mixture for 90 minutes (extraction tower Residence time) during extraction treatment (total operation time of the extraction process: 600 minutes) to remove asphaltene to remain in the raffinate, and to recover the oil and solvent mixture by volatilization, and then to separate the solvent from the recovered oil and solvent mixture. 958,000 L of low sulfur fuel oil was obtained. The sulfur content, asphaltene content, yield, spot rating by the spot test immediately after removal of asphaltene, and the spot rating with time change by the spot test were measured in the obtained ultra-low sulfur fuel oil, and these results are shown in Table 1.

[Example 4]

t-AR: t-DAO 1,656,000ℓ of an oily mixture mixed with a volume ratio of 1: 1 was added to the solvent at 42 barg, 220℃ at a ratio of 1, and n-pentane was added in the ratio of the solvent/oil mixture to a volume ratio of 1 for 70 minutes (extraction tower Residence time) during extraction treatment (total operation time of the extraction process: 600 minutes) to remove asphaltene to remain in the raffinate, and to recover the oil and solvent mixture by volatilization, and then to separate the solvent from the recovered oil and solvent mixture. 1,495,000 liters of low sulfur fuel oil were obtained. The sulfur content, asphaltene content, yield, spot rating by the spot test immediately after removal of asphaltene, and the spot rating with time change by the spot test were measured in the obtained ultra-low sulfur fuel oil, and these results are shown in Table 1.

[Comparative Example 1]

Instead of mixed oil, 1,325,000ℓ of t-AR single oil was added as a solvent under the condition of 42 barg, 190℃, and n-pentane was added in the ratio of the solvent/oil mixture volume ratio of 3, followed by extraction treatment for 70 minutes (extraction tower residence time). Total operation time of the process: 600 minutes) After removing asphaltene to remain in the raffinate and recovering the oil and solvent mixture by volatilization, the solvent was separated from the recovered oil and solvent mixture to obtain 1,176,000 L of ultra-low sulfur fuel oil. The sulfur content, asphaltene content, yield, spot rating by the spot test immediately after removal of asphaltene, and the spot rating with time change by the spot test were measured in the obtained ultra-low sulfur fuel oil, and these results are shown in Table 2.

[Comparative Example 2]

The sulfur content, asphaltene content, and spot rating of the low-sulfur AR single oil without asphaltene removal were measured, and these results are shown in Table 2. Here, the low sulfur AR is not desulfurized, but is an atmospheric residual oil (AR) with a low sulfur content.

[Comparative Example 3]

Low sulfur AR: Measure the sulfur content, asphaltene content, Spot Rating by Spot Test and Spot Rating with time change by Spot Test, without removing asphaltene from the oily mixture mixed with ULSD at a volume ratio of 91:9. These results are shown in Table 2.

[Comparative Example 4]

Low sulfur AR: Measure the sulfur content, asphaltene content, Spot Rating by Spot Test and Spot Rating with time change by Spot Test, without removing asphaltene from the oily mixture in which ULSD is mixed at a volume ratio of 76: 24. These results are shown in Table 2.

[Comparative Example 5]

Low sulfur AR: ULSD: UCO in a volume ratio of 91:4.5:4.5 without removing asphaltene, sulfur content, asphaltene content, spot rating by spot test immediately after mixing, and change with time by spot test spot rating Was measured, and these results are shown in Table 2.

[Comparative Example 6]

Low sulfur AR: ULSD: SLO in volume ratio 72: 20: 8 without removing asphaltene, sulfur content, asphaltene content, spot rating by spot test immediately after mixing, and change with time by spot test spot rating Was measured, and these results are shown in Table 2. Here, SLO is the residue of the FCC (Fluidized Catalytic Cracking) process.

[Comparative Example 7]

t-AR: LCO: SLO: H-Aro in volume ratio 80: 9: 6: 5 without removing asphaltene, sulfur content, asphaltene content, spot rating and spot by spot test immediately after mixing The spot rating of change over time was measured by the test, and these results are shown in Table 2. Here, LCO is a kind of inexpensive oil produced in the fluidized bed catalytic reaction process, and H-Aro is a by-product in the aromatic production process.

In Tables 1 and 2, S% represents the sulfur content, AS% represents the asphaltene content, and S.R. represents the Spot Rating. In Table 2, i means immediately after mixing, which indicates that the stability over time was not confirmed due to high Spot Rating immediately after mixing.

When explaining the effects of the present invention based on the results shown in Tables 1 and 2 are as follows:

1. It can be seen that all of the examples in which asphaltene was removed from the mixed oil showed high stability after removing the asphaltene from the low stability before removing the asphaltene, and it is believed to prove the stability of the mixed oil according to the present invention. In addition, it was confirmed that the stability over time was also significantly improved by showing a Spot Rating of 1 without any change over time even in more than 30 days in the stability over time of the mixed oil by removing asphaltene.

2. Example 1, in which asphaltene was removed from the mixed oil containing t-AR, was compared with Comparative Example 1 in which asphaltene was removed from the t-AR alone oil. It was confirmed that the stability was shown, and the yield was improved by increasing the reaction temperature even though the amount of the solvent used was reduced.

3. When comparing Example 2 in which asphaltene was removed from the same mixed oil with Example 1, it was confirmed that the yield was improved by lowering the reaction temperature despite the amount of the same solvent used. This is analyzed to show that the yield can vary depending on the density of the solvent in the supercritical state in the extraction column during the period.

4. When comparing Example 4 in which asphaltene was removed from the same mixed oil with Example 3, in spite of the same amount of solvent used, Example 4 using n-pentane compared to Example 3 using i-pentane It was confirmed that the yield was greatly improved. This is also analyzed to show that the yield may vary depending on the density of the supercritical solvent in the extraction column depending on the presence or absence of branching of the solvent.

5. In the case of Comparative Examples 2 and 3 in which asphaltene was not removed, the Spot Rating was 1 immediately after mixing, showing stability, but in terms of aging stability, the Spot Rating decreased to 2 after 14 to 18 days of mixing.

6. In the case of Comparative Examples 4 and 5 in which asphaltene was not removed, the Spot Rating was 2 immediately after mixing, but the Spot Rating decreased to 3 after 14 to 18 days of mixing in terms of aging stability. Therefore, it was confirmed that the comparative examples (Comparative Examples 2 to 5) showing relatively high stability immediately after mixing showed a decrease in stability over time.

7. The mixed oils of Comparative Examples 6 and 7 which did not remove asphaltene and contained an oil having a high asphaltene content showed low stability even immediately after mixing.

8. Although, in the above examples, only the mixed oil was described using only t-AR and t-DAO, similar results could be obtained for other oils, as listed above, remaining after producing high-quality oil. there was.

Although the present invention has been described with reference to specific embodiments so far, various modifications are possible without departing from the scope of the present invention. Therefore, the scope of the present invention should not be limited to the described embodiments and should not be defined by the claims to be described later, as well as by the claims and their equivalents.

Claims (9)

(1) a mixing step of producing a high-quality oil in a petroleum refining process and mixing the remaining at least two types of oil to obtain an oil mixture;
(2) asphaltene, which is recovered by adding a hydrocarbon solvent having 3, 4 or 5 carbon atoms to the oil mixture and heating to extract and separate asphaltene from the oil mixture, remaining in the raffinate, and volatilizing the mixture of the oil component and the solvent. Separation step; And
(3) a refinery step of removing the hydrocarbon solvent from the recovered mixture of oil and solvent to obtain ultra-low sulfur fuel oil;
Consisting to include, and manufacturing an ultra-low sulfur fuel oil having a sulfur content of 0.5% by weight or less based on the total weight, a method of producing an ultra-low sulfur fuel oil. The method of claim 1,
The oil is AR (Atmospheric Residue; atmospheric pressure residual oil), VR (Vacuum Residue; decompression residual oil), t-AR (hydrotreated Atmospheric Residue; desulfurization atmospheric pressure residual oil), t-VR (hydrotreated Vacuum Residue; desulfurization and decompression residual oil) , DAO (Deasphalted Oil; deasphalted oil), t-DAO (hydrotreated Deasphalted Oil; desulfurized and deasphalted oil), UCO (Unconverted Oil; unconverted oil (or HCR process residue), VGO (Vacuum Gas Oil; reduced pressure gas oil) , t-VGO (hydrotreated VGO, desulfurized decompression gas oil), HSD (High sulfur Diesel; high sulfur diesel oil), ULSD (Ultra Low Sulfur Diesel; ultra low sulfur diesel oil), characterized in that it is selected from the group consisting of, ultra-low sulfur fuel How to make oil. The method according to claim 1 or 2,
The hydrocarbon solvent used in the asphaltene separation step is selected from the group consisting of n-propane, n-butane, i-butane, n-pentane, i-pentane, and mixtures of two or more thereof. Manufacturing method. The method according to claim 1 or 2,
The asphaltene separation step adds 1 to 4 times the volume of the oil mixture with a hydrocarbon solvent having 3, 4 or 5 carbon atoms at a pressure in the range of 30 to 50 barg and a temperature in the range of 100 to 230°C in the extraction tower (hydrocarbon Solvent: mixed oil = 1 to 4: 1), characterized in that the reaction, the method for producing ultra-low sulfur fuel oil. The method of claim 4,
Preparation of ultra-low sulfur fuel oil, characterized in that the hydrocarbon solvent used in the asphaltene separation step is selected from the group consisting of n-propane, n-butane, i-butane, n-pentane, i-pentane, and mixtures of two or more thereof Way. After producing high-quality oil in the petroleum refining process, a hydrocarbon solvent having 3, 4 or 5 carbon atoms is added to the oil mixture obtained by mixing at least two oils remaining, followed by heating to extract and separate asphaltene from the oil mixture into raffinate. After remaining, the mixture of the oil component of the oil mixture and the hydrocarbon solvent is recovered by volatilization, and then obtained by removing the hydrocarbon solvent from the mixture of the recovered oil component and the solvent, a sulfur content of 0.5% by weight or less based on the total weight is obtained. Eggplant, ultra-low sulfur fuel oil. The method of claim 6,
The oil is selected from the group consisting of AR, VR, t-AR, t-VR, DAO, t-DAO, UCO, VGO, t-VGO, HSD, and ULSD. The method of claim 6,
Ultra-low sulfur fuel oil, characterized in that it has an asphaltene content in the range of 0.01 to 0.6% by weight based on the total weight. An ultra-low sulfur fuel oil obtained by the method for producing an ultra-low sulfur fuel oil according to any one of claims 1 to 5, and having a sulfur content of 0.5% by weight or less based on the total weight.

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