KR100841805B1 - Method for producing feedstocks of high quality lube base oil from coking gas oil - Google Patents

Abstract

A method for manufacturing feedstocks of high quality lube base oil from CGO is provided to improve economic efficiency greatly by using the CGO with a low utility value, and to maximize efficiency by recycling UCO(unconverted oil) of fuels hydrocracker. A method for manufacturing feedstocks of high quality lube base oil comprises the steps of: separating VGO(vacuum gas oil), VR(vacuum residue), or a mixture(VR/AR) of AR(atmospheric residue) and the VR from the AR, and supplying the VGO to a hydrotreating unit(HDT) and the VR or the mixture to a first fractional distillation process(Fs1); obtaining CGO by performing a coking process of the VR or mixture, and supplying the obtained CGO with the VGO to the hydrotreating unit; removing impurities in the hydrotreating unit; obtaining light and heavy hydrocarbon through a hydrocracking unit(HDC); separating an oil product and UCO from the hydrocarbon; obtaining the feedstocks of high quality lube base oil and residue UCO; and recycling the obtained UCO to the hydrocracking unit.

Description

Method for producing feedstocks of high quality lube base oil from coking gas oil}

The present invention relates to a method for producing a high-grade lubricating base oil feedstock using a coker gas oil (CGO), and more specifically, to the reduced pressure gas oil (VGO) used in the conventional hydrogenation process, coker gas oil (CGO) ) And a process for producing an advanced lubricating base oil feedstock by performing a fuel oil hydrotreating process and hydrocracking process and recycling the unconverted oil (UCO) generated therefrom.

The process of manufacturing the lubricating base oil feedstock in connection with the conventional fuel oil hydrocracking process is a method using the unconverted oil (UCO) generated by hydrocracking the reduced pressure gas oil (VGO) produced in the vacuum distillation process (V1), First, it undergoes a hydrotreatment reaction process (HDT) to remove impurities such as sulfur, nitrogen, oxygen and metals contained in the oil, and then converts a considerable amount into light hydrocarbons while passing through a hydrocracking reaction process (HDC), which is a main reaction process. In the process, a series of fractional distillation processes (Fs) separate the decomposed various oils and gases to produce light oil. In the above reaction, the reaction conversion rate per pass is generally designed to be about 40%, and it is practically impossible to operate the conversion rate per pass at 100%, so that unconverted oil (UCO) is always generated in the last fractionation process. Part of it is taken out and used as raw material for lubricating base oil and the rest is recycled to hydrocracking reaction process.

90% of unconverted unconverted oil (UCO), which is a by-product, because aromatics, sulfur compounds, coral compounds, and nitrogen compounds contained in a large amount of reduced pressure gas oil (VGO) are saturated by hydrogen during the hydroprocessing reaction process. Since the above becomes a saturated hydrocarbon, it becomes an oil having a high viscosity index, which is one of the most important characteristics in lubricating base oil properties.

In this regard, the present applicant directly extracts unconverted oil (UCO) from a recycle mode operation of a reduced pressure gas oil (VGO) fuel oil hydrocracking process in Korean Patent Publication No. 96-13606 and provides it as a feedstock for producing lubricant base oil. It is not necessary to recycle the process (reduced pressure distillation of atmospheric pressure residue) to reduce the amount (load) of the first reduced pressure distillation process and the hydroprocessing and hydrocracking reaction process to produce an effective fuel oil and high grade lube base oil feedstock. The method is presented. Accordingly, compared to the conventional fuel oil hydrocracking process in which unconverted oil (UCO) is recycled in a first vacuum distillation process or a hydrocracking reaction process without using the lubricating base oil feedstock, a method of producing the lubricating base oil feedstock Although it is possible to manufacture high quality lubricant base oils having a viscosity of 100N and 150N while greatly removing the inefficiency, it is designed to use only reduced pressure gas oil (VGO), and together with low cost coker gas oil (CGO) No economic considerations have been given to making the feedstock of higher lubrication base oils more economical by using and recycling unconverted oil (UCO).

Accordingly, the present applicant has repeatedly studied to maximize the efficiency and economic efficiency of the above-described method for producing a feedstock of high-grade lubricant base oil, coke gas oil (CGO) as a vacuum residue (VR) or atmospheric pressure residue and vacuum residue oil It can be produced from a mixture of (VR / AR) and mixed with reduced-pressure gas oil (VGO) to hydroprocess and hydrocracking reaction, and then recycled unconverted oil (UCO) generated from it to produce a feedstock of high-grade lubricant base oil. I came up with a way.

Accordingly, an object of the present invention is to significantly improve the economics by utilizing a low value of coker gas oil (CGO), and the high efficiency that can maximize the efficiency by recycling the unconverted oil (UCO) of the fuel oil hydrocracking process It is to provide a method for producing a lubricant base oil feedstock.

The method for producing an advanced lubricating base oil feedstock using coker gas oil (CGO) according to the present invention for achieving the above object, by distilling atmospheric pressure residual oil (AR) in the first reduced pressure distillation process (V1) Oil (VGO) and vacuum residue (VR) or a mixture of atmospheric residue and a mixture of vacuum residue (VR / AR), and the vacuum gas oil (VGO) is supplied directly to the hydroprocessing reaction process (HDT) Supplying the vacuum residue (VR) or a mixture of the atmospheric residue and the vacuum residue (VR / AR) to a first fractional distillation process (Fs1); In the first fractional distillation process (Fs1), the fuel residue is separated, the vacuum residue (VR) or the atmospheric residue oil and the mixture of vacuum residue oil (VR / AR) is supplied to a coker drum to perform a coking process and then again the Obtaining coker gas oil (CGO) through a first fractional distillation process (Fs1) and supplying the coker gas oil (CGO) obtained together with the reduced pressure gas oil (VGO) to a hydroprocessing reaction process (HDT); Removing impurities through the hydrotreating process (HDT); Obtaining light and heavy hydrocarbons through a hydrocracking reaction process (HDC); Supplying the hard and heavy hydrocarbons to a second fractional distillation process (Fs2) to separate the oil product and the unconverted oil; Supplying all of the separated unconverted oil to a second vacuum distillation process (V2) to obtain an advanced lubricant base oil feedstock having a predetermined viscosity grade and remaining unconverted oil; And recycling the unconverted oil obtained from the second vacuum distillation process (V2) to the hydrocracking reaction process (HDC).

Another method for preparing a high-grade lubricating base oil feedstock using the coker gas oil (CGO) according to the present invention for achieving the above object, by distilling the atmospheric residual oil (AR) in the first vacuum distillation process (V1) Decompression gas oil (VGO), and vacuum residue (VR) or a mixture of atmospheric residue and a mixture of vacuum residue (VR / AR), the vacuum gas oil (VGO) is a direct hydroprocessing reaction (HDT) Supplying the vacuum residue (VR) or a mixture of the atmospheric residue and the vacuum residue (VR / AR) to a first fractional distillation process (Fs1); In the first fractional distillation process (Fs1), the coking process is performed by supplying the vacuum residue (VR) or the mixture of atmospheric pressure residue and the vacuum residue (VR / AR) from which the fuel component is separated into a coker drum, and then performing a coking process. Obtaining coker gas oil (CGO) through the first fractional distillation process (Fs1) and supplying the coker gas oil (CGO) to the hydroprocessing reaction process (HDT) together with the reduced pressure gas oil (VGO); Removing impurities through the hydrotreating process (HDT); Obtaining light and heavy hydrocarbons through a hydrocracking reaction process (HDC); Supplying the hard and heavy hydrocarbons to a second fractional distillation process (Fs2) to separate the oil product and the unconverted oil; Supplying the separated unconverted oil to a second vacuum distillation process (V2) to obtain an advanced lubricant base oil feedstock having a predetermined viscosity grade and remaining unconverted oil; And recycling the remaining unconverted oil separated from the second fractional distillation process and the unconverted oil obtained from the second vacuum distillation process (V2) to the hydrocracking reaction process (HDC).

According to the present invention, a coker gas oil (CGO) obtained by performing a coking process on a vacuum residue (VR) or a mixture of atmospheric pressure residue and a vacuum residue (VR / AR) is mixed with a vacuum gas oil (VGO) Hydrogenation and decomposition reaction processes (HDT, HDC) are carried out, and the unconverted oil (UCO) obtained therefrom can be recycled to the hydrocracking reaction process (HDC) to produce a feedstock of high-grade lubricating base oil, which is low and difficult to process. By utilizing coke gas oil (CGO) of the nature it is possible to produce a more economical and efficient high-grade base oil feedstock.

Simple modifications and variations of the present invention can be readily used by those skilled in the art, and all such variations or modifications can be considered to be included within the scope of the present invention.

Hereinafter, with reference to the accompanying drawings of the present invention in more detail as follows.

As described above, FIG. 1 is a hydrocracking process and an advanced lubricator using coker gas oil (CGO) supplied from a coking process and a vacuum gas oil (VGO) supplied from a first vacuum distillation process according to an embodiment of the present invention. As a schematic process chart of a method for producing an oil raw material in a recirculation mode, it is not only using vacuum gas oil (VGO) which is generally used as a raw material for the hydrogenation reaction, but also a vacuum residue or a vacuum residue and a vacuum residue. The mixture (VR / AR) of the first fractional distillation process (Fs1), after the coking process through the coker drum, the coke gas oil (CGO) is produced again through the first fractional distillation process, and then reduced pressure gas oil (VGO) ) And a light feed through a hydrocracking process (HDC) to produce a light fraction, followed by the use of unconverted oil (UCO) to produce an advanced lubricant base oil feedstock.

In more detail, referring to Figure 1, the present invention is distilled from the atmospheric residual oil (AR) separated from the atmospheric pressure distillation process (CDU) in the first vacuum distillation process (V1) to reduce the pressure gas oil (VGO) and the vacuum residue ( VR) or a vacuum gas oil (VGO) and a mixture of vacuum residue oil and a vacuum residue oil (VR / AR), and the vacuum gas oil (VGO) is directly supplied to a hydroprocessing reaction process (HDT). For the vacuum residue (VR) or the mixture of atmospheric residue and the vacuum residue (VR / AR), the first fractional distillation process (Fs1) and the coking process through the coker drum, and again the first fractional distillation process (Fs1) Coke gas oil (CGO) is obtained by performing. The coker gas oil (CGO) thus obtained is supplied to the hydroprocessing reaction process (HDT) together with the reduced pressure gas oil (VGO).

Looking at the coker gas oil (CGO) production process in more detail, the vacuum residue (VR) separated in the first vacuum distillation process (V1) or a mixture of atmospheric pressure residue and the vacuum residue (VR / AR) is made of 1 The fractional low boiling point component is separated through the fractional distillation process (Fs1), and the remaining oil is added to the coker drum and heated rapidly to a sufficient temperature to form coke in the coker drum. Steam is supplied together to maintain minimum velocity and residence time in the chopper and to suppress coke formation. The liquid remaining in the coker drum is converted to coke and light hydrocarbon gas and all gas is discharged to the top of the coker drum. At least two coker drums are required to perform this process, and while the coke is formed on one drum, the other one stops the flow of oil and removes the coke. Coker gas oil (CGO) produced through this coking process is not oxidatively safe and has a high content of HPNA (High Poly-Nuclear Aromatic hydrocarbon) (7 or more aromatic rings). Unconverted oil (UCO), produced by supply, is not suitable as a raw material for high-grade lubricating base oils. However, when the unconverted oil (UCO) is recycled to the hydrocracking process (HDC) as in the method according to the present invention, it is possible to secure a high quality unconverted oil (UCO) having low HPNA content and oxidative stability, and high quality. 100D and 150D grades of lubricating base oil which can be used as raw material of lubricating base oil can be produced to the maximum, and coke gas oil (CGO), which was previously used only as bunker C oil or as raw material for producing diesel fuel (DSL), is an advanced lubricator. By making it possible to use it as a raw material of oil, it has the effect of improving the economics due to high added value.

Specific conditions of the coking process in the method according to the present invention are as shown in Table 1 below.

Operating condition, unit range Heater discharge temperature, ℃ 480-500 Cocker Drum Temperature, ℃ 500-600 Top-cocker drum pressure, psig 15-30 Circulation Ratio (Circulation Volume / Supply Volume) 0.05-0.2

The coker gas oil (CGO) produced from the coking process is mixed with the vacuum gas oil (VGO) and supplied to the hydroprocessing reaction process (HDT), where the coker gas oil (CGO) and the vacuum gas oil (VGO) are mixed. Higher VGO content yields higher lubrication base oil production but increases production cost. Higher CGO content lowers production cost, but coker gas oil (CGO) Since the properties of are not as good as those of the vacuum gas oil (VGO), the mixing volume ratio (VGO / CGO) of the vacuum gas oil (VGO) and the coker gas oil (CGO) is preferably 3 to 9. Representative properties of reduced pressure gas oil (VGO) and coker gas oil (CGO) and unconverted oil (UCO) obtained through the hydrogenation reaction are shown in Table 2 below.

The hydrotreating process (HDT) is a process for removing impurities such as sulfur, nitrogen, oxygen, and metals contained in the feedstock. After the hydrotreating process (HDT), the main reaction process is a hydrocracking reaction process (HDC). The hydrocracking process of) converts significantly to light hydrocarbons. The hydrotreating reaction process (HDT) and hydrocracking reaction process (HDC) may be operated in a once-through mode or recycle mode, and may be one-stage or two-stage. It can be configured in various ways.

The light and heavy hydrocarbons produced through the hydrocracking reaction process (HDC) are fed to a second fractional distillation process (Fs2) and separated into oil products and unconverted oil (UCO). All or part of the separated unconverted oil (UCO) is supplied to the second vacuum distillation process (V2) to separate the high grade lube base oil feedstock having a predetermined viscosity grade and to obtain the remaining amount of unconverted oil (UCO).

In addition, the remaining unconverted oil (UCO) from the second reduced pressure distillation process (V2) is recycled to the hydrocracking reaction process (HDC). On the other hand, when only a part of the gas is selectively supplied to the second vacuum distillation step V2, the remaining unconverted oil UCO from the second fractional distillation step Fs2 is not yet remaining in the remaining amount from the second vacuum distillation step V2. It is recycled to the hydrocracking reaction process (HDC) together with refuel (UCO).

In this case, the ratio of the unconverted oil produced in the second fractional distillation process (Fs2) to the total unconverted oil recycled to the hydrocracking reaction process (HDC) is preferably 3: 1 to 5: 1, and the second reduced pressure The ratio of the unconverted oil supplied to the second vacuum distillation process (V2) to the unconverted oil recycled from the distillation process (V2) to the hydrocracking reaction process (HDC) is preferably 1.3: 1 to 1.5: 1.

The second vacuum distillation process (V2) is operated at a column bottom temperature of 320 to 350 ° C., a column bottom pressure of 140 to 160 mmHg, a column top temperature of 75 to 95 ° C., and a column top pressure of 60 to 80 mm Hg. For the lube base oil feedstock having a predetermined viscosity grade obtained in the distillation process (V2), the dewaxing process and the stabilization process may be further proceeded.

Therefore, according to the present invention, when the same amount of atmospheric residue oil (AR) is supplied to the first reduced pressure distillation process (V1), coker gas oil (CGO) to about 10 to 25% by volume from the vacuum residue (VR) It can be extracted and mixed with vacuum residue (VR) and used as a raw material for hydroprocessing and decomposition reaction processes (HDT, HDC). Therefore, it is about 10 to 30 compared to the case where only conventional vacuum gas oil (VGO) is used as a feedstock. It has the advantage of converting the atmospheric residual oil (AR) of about% to a feedstock of high value-added light oil and high-grade lubricating base oil.

Hereinafter, the present invention will be described in more detail with reference to the following examples, but the scope of the present invention is not limited thereto.

Example  One

The vacuum residue oil (VR) separated from the first vacuum distillation process (V1) using the atmospheric residue oil (AR) as a raw material separates some low boiling point components through the first fractional distillation process (Fs1) and is heated to 500 ° C. And into the cocker drum. The liquid remaining in the drum, heated to a temperature of 550 ° C and a top coker drum pressure of 25 Psig in the coker drum, was converted to coke and light hydrocarbon gas, and all gases were converted to LPG, Gas, Naphtha, It was separated into coker gas oil (CGO). Coker gas oil (CGO) and reduced pressure gas oil (VGO) having the properties shown in Table 2 are LHSV (Liquid Hourly Space Velocity) 3.429 hr ⁻¹ , pressure 2397 Psig, temperature 385.8 ° C., in a hydrotreating reaction process (HDT). The catalyst was treated using UF-210STARS (manufactured by UOP Co., Ltd.) under a condition of hydrogen inflow rate of 842 Nm ³ / m ³ , followed by LHSV 1.241 hr ⁻¹ , pressure 2397 Psig, and temperature 395.2 ° C. with recycled UCO described below. The UF-210 / HC-115 / UF-100 catalyst (manufactured by UOP Co., Ltd.) was treated in a VGO / CGO hydrocracking process (HDC) under a hydrogen inflow rate of 1180 Nm ³ / m ³ .

Subsequently, diesel and light products having a boiling point of 350 ° C. or lower were recovered through a conventional fractional distillation process, and unconverted oil (UCO) having the properties shown in Table 2 was obtained, and injected into a UCO vacuum distillation process (V2) to determine the top pressure. Distilled under reduced pressure at 75 mmHg, tower top temperature 80 ℃ and tower bottom pressure 150mmHg, tower bottom temperature 325 ℃ Light Distillate 36.3 LV%, 100N extract 33.4 LV%, Middle Distillate 10.5 LV % And 19.8 LV% of 150N extract, which is a bottom product, was obtained.

Only 100N and 150N extracts were taken out as 53.2% (ie, 100N: 33.4% and 150N: 19.8%) of the supply amount (ie, 100N: 33.4% and 150N: 19.8%) as intermediate products, and the rest (46.8% of the supply amount) were summed together to produce Recycled to (HDC). This resulted in the production of 100N and 150N grade high viscosity index, low volatility high grade lubricating base oils as shown in Table 3, and by accumulating 53.2% of UCO, cumulative prevention of refractory components and polynuclear aromatic compounds is automatically achieved. By providing extra capacity for V1 and HDT, it has been proven that the facility can be used very efficiently by providing additional processing capacity as much as the amount of lubricant base oil production.

Comparative example

The vacuum gas oil (VGO) having the properties shown in the above [Table 2] is separated from the first vacuum distillation process (V1) by using the atmospheric residual oil (AR) as a raw material, and the LHSV (Liquid) in the hydroprocessing reaction process (HDT). Hourly Space Velocity) After hydrogenation using UF-210STARS (manufactured by UOP) as a catalyst under the conditions of 3.429 hr ^-1 , pressure 2397 Psig, temperature 385.8 ° C., hydrogen inflow rate 842 Nm ³ / m ³ , the recycling described later With UCO and LHSV 1.241 hr ^-1 , pressure 2397 Psig, temperature 395.2 ° C using UF-210 / HC-115 / UF-100 catalyst (manufactured by UOP) at a hydrogen flow rate of 1180 Nm ³ / m ³ Treatment was carried out in a hydrocracking reaction process (HDC).

Subsequently, diesel and light products having a boiling point of 350 ° C. or lower were recovered through a conventional separator and several fractional distillation processes to obtain unconverted oil (UCO) having the properties shown in Table 4 below, which was subjected to a UCO vacuum distillation process (V2). Injected by distillation under reduced pressure to a column top pressure of 75 mmHg, tower top temperature of 80 ℃ and tower bottom pressure of 150 mmHg, tower bottom temperature of 325 ℃ light distillate 32.5LV%, 100N extract 34.8LV%, intermediate extract ( Middle Distillate) 14.6LV% and 150N extract of the bottom product 18.1LV%.

Among them, only 100N and 150N extracts were taken out of 52.9% (that is, 100N: 34.8% and 150N: 18.1%) of the supply amount (ie, 100N: 34.8% and 150N: 18.1%) as intermediate products, and the rest (47.1% of the supply amount) were summed together. HDC). Through this, a high viscosity index, low volatile high-grade lubricant base oil raw material of 100N and 150N grades as shown in Table 4 was produced.

Comparing the embodiment according to the present invention and the comparative example according to the prior art, the conditions of the hydrocracking process applied to both examples are similar, but unlike the comparative example using only reduced pressure gas oil (VGO) as a feedstock In the exemplary embodiment of the present invention, 10-25% of coker gas oil (CGO) prepared from vacuum residue (VR) or a mixture of vacuum residue and atmospheric pressure residue (VR / AR) is mixed with vacuum gas oil (VGO). It can be used as a raw material, and by recycling the unconverted oil generated from this by hydrocracking reaction process (HDC), it is possible to produce a raw material of lubricating base oil of similar properties as the prior art, about 10 to 30 compared to the comparative example according to the prior art It will be able to replace about VGO. That is, based on the same amount of atmospheric residual oil (AR), it is possible to produce more feedstock of light oil and high-grade lubricating base oil of high added value compared to the comparative example according to the prior art.

1 is a schematic process diagram of producing a fuel oil hydrocracking process and a lubricating base oil feedstock in recycle mode according to an embodiment of the present invention.

<Description of the symbols for the main parts of the drawings>

CGO: Coker Gas Oil VGO: Decompression Gas Oil

UCO: unconverted oil CDU: atmospheric distillation process

AR: Pressure Residual Oil VR: Pressure Residual Oil

V1: first reduced pressure distillation step V2: second reduced pressure distillation step

HDT: Hydroprocessing Reaction Process HDC: Hydrocracking Reaction Process

Fs1: first fractional distillation process Fs2: second fractional distillation process

Claims (5)

The atmospheric residue oil (AR) is distilled from the first vacuum distillation process (V1), and separated into vacuum gas oil (VGO), and vacuum residue oil (VR) or a mixture of atmospheric residue and vacuum residue (VR / AR). The vacuum gas oil (VGO) is directly supplied to a hydroprocessing reaction process (HDT), and the vacuum residue (VR) or a mixture of atmospheric pressure residue and a vacuum residue oil (VR / AR) is a first fractional distillation process ( Feeding to Fs1); In the first fractional distillation process (Fs1), the coking process is performed by supplying the vacuum residue (VR) or the mixture of atmospheric pressure residue and the vacuum residue (VR / AR) from which the fuel component is separated into a coker drum, and then performing a coking process. Obtaining coker gas oil (CGO) through the first fractional distillation process (Fs1) and supplying the coker gas oil (CGO) obtained together with the reduced pressure gas oil (VGO) to the hydroprocessing reaction process (HDT); Removing impurities through the hydrotreating process (HDT); Obtaining light and heavy hydrocarbons through a hydrocracking reaction process (HDC); Supplying the hard and heavy hydrocarbons to a second fractional distillation process (Fs2) to separate the oil product and the unconverted oil; Supplying all of the separated unconverted oil to a second vacuum distillation process (V2) to obtain an advanced lubricant base oil feedstock having a predetermined viscosity grade and remaining unconverted oil; And Recycling the unconverted oil obtained from the second vacuum distillation step (V2) to the hydrocracking reaction step (HDC), characterized in that the manufacturing method of the advanced lubricant base oil feedstock using coker gas oil (CGO). The atmospheric residue oil (AR) is distilled from the first vacuum distillation process (V1), and separated into vacuum gas oil (VGO), and vacuum residue oil (VR) or a mixture of atmospheric residue and vacuum residue (VR / AR). The vacuum gas oil (VGO) is directly supplied to a hydroprocessing reaction process (HDT), and the vacuum residue (VR) or a mixture of atmospheric pressure residue and a vacuum residue oil (VR / AR) is a first fractional distillation process ( Feeding to Fs1); In the first fractional distillation process (Fs1), the coking process is performed by supplying the vacuum residue (VR) or the mixture of atmospheric pressure residue and the vacuum residue (VR / AR) from which the fuel component is separated into a coker drum, and then performing a coking process. Obtaining coker gas oil (CGO) through the first fractional distillation process (Fs1) and supplying the coker gas oil (CGO) obtained together with the reduced pressure gas oil (VGO) to the hydroprocessing reaction process (HDT); Removing impurities through the hydrotreating process (HDT); Obtaining light and heavy hydrocarbons through a hydrocracking reaction process (HDC); Supplying the hard and heavy hydrocarbons to a second fractional distillation process (Fs2) to separate the oil product and the unconverted oil; Supplying the separated unconverted oil to a second vacuum distillation process (V2) to obtain an advanced lubricant base oil feedstock having a predetermined viscosity grade and remaining unconverted oil; And Coker gas oil comprising the step of recycling the remaining unconverted oil separated from the second fractional distillation (Fs2) and the unconverted oil obtained from the second reduced pressure distillation (V2) to the hydrocracking reaction process (HDC). Process for preparing advanced lubricant base oil feedstock using (CGO). The mixed volume ratio (VGO / CGO) of the reduced pressure gas oil (VGO) and the coker gas oil (CGO) supplied to the hydroprocessing reaction process (HDT) is 3 to 9. Method for producing high-grade lubricating base oil feedstock using coker gas oil (CGO). According to claim 1 or 2, wherein the ratio of the unconverted oil produced in the second fractional distillation process (Fs2) to the unconverted oil recycled to the hydrocracking reaction process (HDC) is 3: 1 to 5: 1. A process for producing an advanced lubricating base oil feedstock using coker gas oil (CGO). The U.S. feed to the second reduced pressure distillation process (V2) for unconverted oil (UCO) recycled from the second reduced pressure distillation process (V2) to the hydrocracking reaction process (HDC). A process for producing an advanced lubricating base oil feedstock using coker gas oil (CGO), characterized in that the ratio of the conversion oil is 1.3: 1 to 1.5: 1.

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