KR100831813B1 - The method of preparing naphthenic lube base oil from aromatic extract and the naphthenic base oil using the method - Google Patents

Abstract

A method for preparing versatile naphthenic lube oil of excellent performance is provided to make use of an aromatic extract that is produced from the production of paraffin-based lube oil using an atmospheric residue as a material. Versatile naphthenic lube oil is prepared by: modifying an aromatic extract through the addition of hydrogen(HT), the aromatic extract being produced from a solvent de-aromatic process following a first vacuum distillation process(VDU 1) on paraffin-based atmospheric residue; and carrying out a second vacuum distillation process(VDU 2) to separate the modified oil in diverse viscosity levels. The hydrogen addition is carried out under conditions of at least 1.0/hr fluid space speed, 1800psig pressure, and 350deg.C, in presence of a Ni-Mo catalyst.

Description

The method of preparing naphthenic lube base oil from aromatic extract and the naphthenic base oil using the method}

1 is a schematic view showing a process for producing a lead-based lube base oil according to an embodiment of the present invention.

Figure 2 is a schematic diagram showing a process for producing a lead-based lube base oil according to another embodiment of the present invention.

※ Explanation of symbols for main parts of drawing

AR: Pressure residue VDU 1: Pressure distillation process

SDA: Solvent degreasing process VR: Decompression residue

SEU: solvent dearomatic process DAE: distillate fraction aromatic extract

RAE: Residual Aromatic Extract CAE: Complex Aromatic Extract

HT: Hydrogen Reforming Process VDU 2: Vacuum Distillation Process

SDW: Solvent Dropping Process HDF: Hydrogen Finishing Process

FS: Fractional Distillation Process

The present invention relates to a method for producing naphtha lubricating base oil using an aromatic extract and to a naphtha lubricating base oil according to the present invention, and more specifically, to a naphtha-based hydrocarbon compound by a hydrogenation reaction using an aromatic extract by-product as a feedstock for the production of paraffinic base oil. The present invention relates to a method for producing lead-based lube base oil and a lead-based lube base oil.

Traditionally, the lead-based lubricating base oil is obtained by further refining the atmospheric residue oil obtained from the lead-based petroleum oil. Many have been used as starting materials to secure oil products of desired properties. The lead-based lube base oil thus obtained has excellent fluidity and excellent solubility at low temperatures, such as the use of electrical insulating oils where the oils need to function as a heat transfer medium and for insulating functions, as well as for the use of rubber in the process of synthesizing or processing rubber products, or as lead-based oils. It is used as a base oil for lubricating oil products for special applications that require oil. In order to secure such an oil, a desired lead-based lubricating base oil product is generally manufactured using lead-based petroleum crude oil, which is rich in lead-based hydrocarbon components in crude oil itself.

However, since the lead-based lubricating base oil according to the prior art is finally obtained from the lead-based crude oil, the economic performance and the performance characteristics of the product is determined according to the economic security of the crude oil as the first raw material and the properties of the crude oil. In addition, current lead-based crude oil reserves represent only 2-3% of the world's oil reserves, and geographical locations include Venezuela, the United States (Texas, California, Louisiana, and Arkansas), the North Sea of the United Kingdom, China (Balhae Bay, Gabor, Yoha, As a result, the supply of lead-based crude oil is becoming more and more difficult. As a result, the world's leading petroleum companies, Exxon, Sun, Chevron, Texaco and Shell, have shut down their lead-based lube base oil plants for the past 15 years. As such, it is difficult to economically secure lead-based lube base oil based on lead-based crude oil, and the price is rising due to the failure to smoothly supply lead-based base oil.

The definition of lead-based oils is not precisely defined due to the nature of the petroleum industry. It is conventionally rich in lead-based hydrocarbons derived from naphtha crude oil and has the following characteristics.

Paraffinic carbon ratio is 55 to 60% or less.

Specific gravity value is 0.876 or more and 0.934 or less.

Excellent solubility compared to paraffinic oil.

Excellent low temperature fluidity due to less wax content than paraffinic oil.

Excellent thermal conductivity compared to paraffinic oils.

Higher volatility than paraffinic oils.

Compared to paraffinic oil, which can supply abundant raw materials, which account for 97-98% of the world's petroleum oil, lead-based oil is becoming more rare. Therefore, it is necessary to find a new feedstock for the production of lead-based oil and to develop a manufacturing technology using the same.

Accordingly, in the present invention, as a result of earnest research to economically secure lead-based lubricating base oil from paraffinic crude oil, which is easy to source raw materials, paraffin-based lubricating oil is used as a feedstock. It was confirmed that economical lead-based lube base oils of various viscosity grades can be prepared by performing hydrogenation reaction and reduced pressure distillation process using the aromatic extract produced from the solvent dearomatic process, which is a unit process, as a feedstock.

Accordingly, an object of the present invention is to economically produce lead-based lube base oil having excellent performance as a feedstock with aromatic extracts from the paraffin-based lube base oil manufacturing process using the atmospheric residue of paraffin-based crude oil having abundant raw materials as a feedstock. To provide a way to do that.

Still another object of the present invention is to provide a lead-based lube base oil that is used for various purposes by using the above production method.

According to the present invention, a method for preparing a lead-based lube base oil according to the present invention includes hydrogenation of aromatic extracts from the first vacuum distillation process (VDU1) and solvent de-aromatic process (SEU) for paraffinic atmospheric residue oil. Modifying (HT); And

And a second vacuum distillation step (VDU2) for separating the reformed fraction into various viscosities.

The lead-based lube base oil for achieving the above another object has a kinematic viscosity at 40 ° C. of 6 centistokes or more and 750 centistokes or less, specific gravity 0.876 to 0.934, and exhibits a paraffinic carbon ratio of 55% or less.

Hereinafter, the present invention will be described in more detail with reference to the accompanying drawings.

As illustrated in FIG. 1, a method for preparing a lead-based lubricant base oil according to the present invention includes a process for preparing a conventional paraffinic lubricant base oil, that is, a reduced pressure distillation process (VDU1) of a paraffinic atmospheric residue oil, and a solvent de-aromatic process (SEU). ), Hydrogenated aromatic extracts from the solvent de-aromatic process (SEU) in the manufacturing process of paraffinic lubricating base oil including solvent desorption process (SDW), hydrofinishing process (HDF) and fractional distillation process (FS). Use as a feedstock for the reaction provides a more economical method for producing lead-based lube base oil.

Hereinafter, the present invention will be described in more detail for each process.

As described above, the feedstock according to the present invention uses an aromatic extract by-produced in a solvent dearomatic process (SEU) during the manufacturing process of the paraffinic base oil, and materials other than the separated aromatic extract are conventional paraffinic base oil processes. Is introduced.

In the present invention, the 'aromatic extract' is a kinematic viscosity of 170 to 5,100 centistokes at 40 ° C. which is by-produced in a solvent dearomatic process for preparing a lubricating base oil using atmospheric residue obtained when distilling petroleum crude oil. An aromatic hydrocarbon mixture of at least 0.98 and an aromatic content of at least 70% by weight.

Among the aromatic extracts, the aromatic by-products obtained from distillate (Distillate) are called Distillate Aromatic Extract (DAE), and the aromatic by-products obtained from vacuum residue are called Residue Aromatic Extract (RAE). do.

On the other hand, when performing a composite aromatic extract (CAE, Composite Aromatic Extract) mixed with several aromatic extracts according to the present invention as a feedstock, it is possible to secure various viscosity grade naphtha lube base oil at the same time, the composite aromatic extract is a conventional paraffinic lubricator As an aromatic extract of a conventional commercial plant generated by the aromatic extracts from the oil plant collected in one storage tank, the following Table 1 is the characteristics of the composite aromatic extract sample of Nippon Oil Corporation (Nippon Oil Corporation), which will be described later. It was used as a feedstock of Example 3.

CAE 1  Specific Gravity @ 15/4 ℃ 0.998  Kinematic Viscosity @ 40 ℃, cSt 560.4  Pour point, ℃ 17.5  Flash point, ℃ 260  Sulfur content, wt% 5.0  Aromatic hydrocarbons, wt% 91.3  Polyaromatic content, wt% 21

These complex or mono-type aromatic extracts are sent to a hydrogenation reaction (HT) to convert the aromatic hydrocarbon structure into a lead-sensed hydrocarbon under hydrogenation catalyst and hydrogen inflow. The hydrogenation catalyst usable here is nickel-tungsten ( Ni-W), nickel-molybdenum (Ni-Mo), and the like, a double nickel-molybdenum-based (Ni-Mo) catalyst may be preferably used, and the liquid hourly space velocity (LHSV) is 1.0 under hydrogen inflow. / hr or less, preferably 0.5 to 1.0 / hr, the pressure is 1,800 psig or more, preferably 2,000 to 2,400 psig, and is treated under conditions of a temperature of 350 ° C or more, preferably 380 to 400 ° C.

At this time, when the fluid space velocity exceeds 1.0 / hr, the reaction pressure is less than 1,800 psig, or the reaction temperature is less than 350 ℃ it is not preferable to convert the aromatic hydrocarbon to lead-sen hydrocarbon because the hydrogenation reaction is not performed sufficiently.

After the hydrogenation reaction, the carbon number of the paraffinic hydrocarbon is 55% or less, the kinematic viscosity at 40 ℃ 6 to 750 centistokes, the specific gravity 0.876 to 0.934 is modified to an oil, which is a separate vacuum distillation process (hereinafter, ' 2 'distillation under reduced pressure distillation process': VDU2) to be separated into various viscosity grades suitable as lead-based lubricating base oil. The second reduced pressure distillation process (VDU2) has a column top pressure of 70 to 80 mmHg, tower top temperature of 70 to 90 ° C, and tower low pressure. 140 to 160 mmHg, the bottom temperature is performed at 300 to 360 ℃. The second reduced pressure distillation process meets the general reduced pressure distillation process conditions in the art.

According to the present invention, a method for preparing lead-based lube base oil includes, after the second reduced pressure distillation process, a solvent dewaxing step (SDW), a hydrogenation finishing reaction step (HDT), and a fractional distillation step (FS) in consideration of the purpose of use of the lubricant base oil. It is preferable to further optionally include one or more of the post-treatment step consisting of the order of. That is, the lubricating base oil which has undergone the second reduced pressure distillation step in the post-treatment process is a process of solvent dewaxing step (SDW), hydrofinishing step (HDT), fractional distillation step (FS) as disclosed in FIG. It is possible to be individually introduced into the post-treatment to the desired properties or conditions, and after the solvent dewaxing step (SDW) to obtain a higher quality product, the hydrofinishing step (HDT) and / or fractional distillation step (FS) It may be rough, may be subjected to the fractional distillation step (FS) after the hydrofinishing step (HDT), it may be designed to pass all of the post-treatment step in accordance with the process sequence.

All or a part of the oil that has undergone the second pressure-reduced fractionation process, a straight-chain paraffinic hydrocarbon compound, such as wax to reduce the fluidity in order to ensure low-temperature fluidity according to the use of the solvent stripping process of the conventional paraffinic lubricant base oil process ( SDW) so that the pour point is below -12.5 ℃. Solvents usable in the solvent dewaxing process include methyl-isobutyl-ketone, propane, methyl-ethyl ketone, and the like. Methyl-ethyl ketone (MEK) may be preferably applied. Meanwhile, the mixing ratio of the oil to the solvent is 2.0 to 3.0, which is performed by mixing and cooling to remove the wax component that inhibits the fluidity of the oil through a two-stage filter.

Also, depending on the application, polycyclic aromatic compounds and hetero (polycyclic aromatic compounds) and hetero ( Sulfur, nitrogen, oxygen, etc.) compounds, such as palladium, nickel-tungsten catalyst may be used in the hydrogenation finishing process, but preferably nickel-tungsten-based ((Ni-W) catalyst) The process is carried out under the conditions of the fluid space velocity 1.0 ~ 2.0 / hr, pressure 1,500 ~ 2,500 psig, preferably 1,900 ~ 2,200 psig, temperature 180 ~ 320 ℃, preferably 220 ~ 280 ℃ under hydrogen inlet with the catalyst This is carried out, and in order to lower the volatility to improve the safety of fire and handling to remove light oil through a fractional distillation process (FS) to obtain a lead-based lubricating base oil, the lead-based lubrication The vigorous oil will have properties and compositions that are equal to or greater than products made from conventional leaded crude 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 to the following examples.

<Manufacture example 1>

The aromatic extract as a feedstock of the present invention is injected into the vacuum distillation process (VDU1) as a feedstock to the atmospheric residue remaining at the bottom of the distillation column during atmospheric distillation of the conventional paraffinic crude oil shown in FIG. Distillate was distilled under reduced pressure at a temperature of 80 ° C. and a tower bottom pressure of 150 mmHg, and a tower bottom temperature of 350 ° C. to extract 12.0% by volume of 60D (Distillate), 15.5% by volume of 100D, 15.5% by volume of 150D, 14.2% by volume of 500D and 150VR (Vacuum) Residue, 42.0LV% of distilled oil and distilled oil of various viscosity grades were obtained and stored as semi-finished products in their respective storage tanks. Solvent de-aromatic process (SEU) as a solvent by applying fufural (Fufural) for the 60D, 100D, 150D, 500D distillates (Vacuum Residue) 150VR mixing ratio of the oil to the solvent 2.2 ~ 4.0, oil temperature 83 ~ 84 ℃, solvent temperature 118 ~ 128 ℃, dearomatic fraction reduced aromatic hydrocarbons are obtained in 58 ~ 75 volume% yield, and these dearomatic fractions are semi-finished products of paraffinic base oil. do. The applied purulent solvent contains the extracted aromatic compound and is recovered in a separate solvent recovery process, in which the aromatic extract is withdrawn. The five aromatic extracts thus obtained are shown in Table 2 below.

Characteristics of DAEs and RAEs Aromatic extract (raw distillate) DAE 1 (60D) DAE 2 (100D) DAE 3 (150D) DAE 4 (500D) RAE 1 (150VR)  Specific Gravity @ 15/4 ℃ 1.001 1.002 1.004 0.986 0.983  Kinematic Viscosity @ 40 ℃, cSt 178.9 1,158 1,591 3,828 5,087  Pour point, ℃ 27.5 22.5 17.5 12.5 17.5  Flash point, ℃ 242 254 258 274 282 Distillation phase, ℃  Superstore 10% off 50% off 90% off 328 383 424 449 514 355 414 480 535 614 374 440 484 539 630 385 455 543 623 689 386 465 551 626 688  Sulfur content, wt% 3.6 3.9 3.8 3.1 3.1  Aromatic hydrocarbons, wt% 90.2 81.6 86.9 72.3 73.5  Polyaromatic content, wt% 8.2 9.7 10.0 5.3 6.5

The properties and performance test results of the lead-based lube base oil prepared by using the aromatic extract as a feedstock are shown in the following Examples and Comparative Examples.

Specific gravity was carried out in accordance with KS M 2002.

Viscosity was performed according to KS M 2014.

Flash point was conducted according to KS M 2010.

Pour point was conducted according to KS M 2016.

Sulfur content was carried out according to KS M 2027 using ANTEK equipment.

The aniline point was carried out in accordance with KS M 2053.

Distillation phase and carbon number distribution test were carried out in accordance with KS M 2031.

The hydrocarbon composition was carried out according to ASTM D 2140.

The aromatic hydrocarbon content was carried out in accordance with ASTM D 2549.

10) Polycyclic aromatic content was carried out according to IP 346.

<Example 1 and Comparative Example 1>

As shown in FIG. 1, the aromatic extract (DAE-1) was injected into a hydrogenation reactor filled with a nickel-molybdenum-based catalyst (Ni-Mo, HR-448, IFP), and a fluid space velocity of 0.5 / hr under hydrogen inflow. 2,466 psig, treated at a temperature of 370 ° C, injected into a vacuum distillation process (VDU2), distilled under reduced pressure to a column top pressure of 75mmHg, tower top temperature of 80 ° C and tower bottom pressure of 150mmHg, and tower bottom temperature of 325 ° C. The volume% and 47.0 volume% of 100N (Neutral) lubricating base oil products, which are intermediate and bottom extracts, were obtained and their properties are shown in Table 3 in comparison with the properties of the common viscose lubricating base oils of the same viscosity grades prepared from naphtha crude oil.

Example 1 Properties and Compositions of 100N Class Lead-Acid Lubricant Base Oils Prepared from DAE DAE-1 feedstock Example 1 100N Comparative Example 1 100 N Lead-based lube base oil requirements  Specific gravity @ 15/4 ℃ (Note 1) 1.001 0.880 0.898 0.876-0.934  Kinematic Viscosity @ 40 ℃, cSt 178.9 19.2 19.4  Flash point, ℃ 242 182 184  Pour point, ℃ 27.5 -7.5 -37.5  Acid value, mgKOH / g - 0.42 0.07  Aniline point, ℃ - 66.8 63.5  Sulfur content, ppm 3.6% 320 145  Hydrocarbon composition,% Paraffinic hydrocarbon (Cp) Naphthenic hydrocarbon (Cn) Aromatic hydrocarbon (Ca)  ---  52 40 8  46 48 6  55 ~ 60 or less (Note 1)  Polyaromatic content, wt% 8.2 2.1 1.7 -

(Note 1) American Petroleum Institute's classification criteria for lead-sen oil: 0.876 ~ 0.934 specific gravity, Cp 55 ~ 60% or less.

In Example 1, the aromatic compounds of the aromatic extract (DAE1) are modified to be a lead-sensing compound by hydrogenation under the above conditions, and the specific gravity 0.876 to 0.934, which is a requirement of the lead-sensed hydrocarbons defined by the American Petroleum Association, to form a paraffin hydrocarbon. It can be seen that the content is converted to a lead-based oil having a content of 55% or less.

The lead-sensing lube base oil 100N prepared in Example 1 may be applied without any abnormality in a region requiring a general naphtha lube base oil, but it can be seen that the pour point is higher than that of the conventional product of Comparative Example 1 and the acidic substance content is also high. Therefore, in order to safely apply in the case of requiring a low-temperature fluidity and excellent heat or UV stability as needed, further purification is required, which is shown in Example 2.

<Example 2>

In order to lower the pour point of the 100N grade lead-sensing oil prepared in Example 1, the solvent was applied to the conventional solvent stripping process (SDW) shown in FIG. 1 by applying methyl-ethyl ketone (MEK). The mixture was mixed at a mixing ratio of 2.0 and then cooled to -17 ° C to remove wax components that hindered fluidity of the oil through a two-stage filter to obtain dewaxed oil in a yield of 79 to 81% by volume based on -37.5 ° C. In order to reduce the acidity of these fractions and to increase the thermal oxidation stability and ultraviolet stability, the nickel-tungsten-based catalyst (Ni-W, Criterion Co., Ltd.) and the fluid space velocity of 1.2 / hr, pressure 1,800 psig, and temperature 264 under hydrogen inflow Treatment of acidic substances or residual impurities under the conditions of ℃ and fractional distillation (FS) at pressure 75mmHg, column top temperature 67 ℃, column bottom temperature 270 ℃ conditions to remove the light oil to improve the flash point, as shown in Table 3 below One bar As said Genie a lower pour point, heat unstable material to oxidation and ultraviolet light that is, to obtain an improved class napsen 100N base oil to contain less aromatics and acids.

Example 2 100N class lead-acid oil with improved fluidity and computational value Example 1 100N Example 2 100N Comparative Example 1 100 N Lead-based lube base oil requirements  Specific gravity @ 15/4 ℃ (Note 1) 0.880 0.885 0.898 0.876-0.934  Kinematic Viscosity @ 40 ℃, cSt 19.2 19.5 19.4  Flash point, ℃ 182 186 184  Pour point, ℃ -7.5 -37.5 -37.5  Acid value, mgKOH / g 0.42 0.01 0.07  Aniline point, ℃ 66.8 64.8 63.5  Sulfur content, ppm 320 24 145  Hydrocarbon composition,% Paraffinic hydrocarbon (Cp) Naphthenic hydrocarbon (Cn) Aromatic hydrocarbon (Ca)  52 40 8  48 47 5  46 48 6  55 ~ 60 or less--  Polyaromatic content, wt% 2.1 0.8 1.7 -

As a result of removing the wax that inhibits fluidity through the conventional solvent dewaxing in Example 2, the pour point was improved to -37.5 ° C. or less, thereby reducing the content of paraffinic hydrocarbons and simultaneously increasing the content of lead-based hydrocarbons from 40% to 47%. It can be seen that further increases. In addition, as a result of performing a hydrogenation finishing process with a catalyst containing nickel-tungsten metal, polycyclic aromatic compounds and hetero compounds, which are acidic substances, are extremely removed, resulting in low acidity (acid value), excellent thermal stability, UV stability, and carcinogenesis. It can be seen that a lead-based lube base oil product having relatively few polycyclic aromatic compounds, which are precursors of the active substance, can be obtained.

In Examples 1 and 2, a single distillate fractional aromatic extract (DAE-1) was used as a feedstock to produce Napsen lubricating base oil. These results were converted into respective Napsen oils in the same manner using different aromatic extracts as a feedstock. According to the viscosity difference of the feedstock, only the viscosity value of the product will be different. In Example 3 below, a mixed raw aromatic extract (CAE, Composite Aromatic Extract) is used as a feedstock, and a waxsen having several viscosity grades at the same time. Lubrication base oil could be secured.

<Example 3>

The CAE used in Example 3 was used to satisfy the properties of the sample of the composite aromatic extract of Nippon Oil Corporation according to Table 1 described above, using the composite aromatic extract as a feedstock, nickel- molybdenum-based (Ni-Mo, Criterion Co., Ltd. LH-23) After injection into a catalyst-packed hydrogenation reactor, hydrogenation under the conditions of liquid flow rate 0.7 / hr, pressure 2,450psig, and temperature 380 ℃ under hydrogen inlet, reduced pressure as shown in FIG. Distillation under reduced pressure by distillation at 75mmHg tower top pressure, tower top temperature 80 ℃ and tower bottom pressure 150mmHg, tower bottom temperature 360 ℃ by injection into distillation process (VDU2) Volume%, 21.5% by volume of extract from 350 ~ 400 ℃, 22.7% by volume of extract from 400 ~ 440 ℃, 21.8% by volume of extract from 440 ~ 490 ℃, 21.9% by volume of extract from above 490 ℃, and their properties are shown in Table 5 Indicated on .

Example 3 Naphtha Oil of Various Viscosity Grades Prepared from CAE Atmospheric distillation temperature range, ℃ (ISO viscosity grade) ~ 350 (10) 350 ~ 400 (22) 400 ~ 440 (68) 440 ~ 490 (220) 490-(680)  Specific gravity @ 15/4 ℃ (Note 1) 0.877 0.891 0.911 0.926 0.933  Kinematic Viscosity @ 40 ℃, cSt 6.3 24.1 66.1 212.8 750.4  Flash point, ℃ 132 182 254 286 366  Pour point, ℃ -42.5 -12.5 3 12 30  Acid value, mgKOH / g 0.22 0.31 0.37 0.41 0.47  Aniline point, ℃ 49.2 61.3 72.1 83.7 97.2  Sulfur content, ppm 7 11 25 34 65  Hydrocarbon composition,% Paraffinic hydrocarbon (Cp) Naphthenic hydrocarbon (Cn) Aromatic hydrocarbon (Ca)  50 49 1  49 48 3  47 48 5  46 47 7  46 44 10  Polyaromatic content, wt% 0.5 0.8 1.4 2.2 2.7

As a result of the hydrogenation reforming and vacuum distillation as a feedstock, the complex aromatic extract according to the present invention was able to secure various viscosity grades of lead-based lubricating base oil. The carbon number constituting the paraffinic hydrocarbon is 46 ~ 50% as a percentage, and satisfies the Cp content of 55 ~ 60%, which is the classification standard of the lead oil of the American Petroleum Institute, and the specific gravity range of the conventional lead-based lubricant base oil is 0.876 or more and 0.934 or less. It was found that the 40 ° C kinematic viscosity value of 6.0 centistokes to 750 centistokes in the range of lead-based oil can be obtained. In addition, the polycyclic aromatic compound, which is a precursor of a carcinogenic substance whose total content of oil is regulated to 3% or less in Europe, is contained in the oil produced by the present invention under the European regulatory value, thereby ensuring environmentally friendly products.

It can be seen that the fluidity is also bad as the viscosity value of the oil is increased in Example 3, when it is necessary to ensure the fluidity at low temperature according to the application purpose, the conventional solvent dewaxing shown in Figure 1 as in Example 2 according to the present invention By carrying out the process, it is possible to secure products with improved fluidity.In order to reduce acidity, and to further improve thermal oxidation stability and ultraviolet ray stability, as in Example 2, hydrogenated finishing process is performed to secure improved products. It is possible.

As described above, according to the present invention, compared to the conventional technique of securing a lead-based lubricating base oil directly from depleted lead-based crude oil, by-products of the conventional paraffinic lubricating base oil manufacturing process from paraffin crude oil, which can supply abundant raw materials, Lead-based lube base oil can be secured economically.

Claims (7)

Reforming the aromatic extract by-product from the solvent dearomatic process (SEU) after the first vacuum distillation process (VDU1) for the paraffinic atmospheric residue oil by hydrogenation (HT); And And a second vacuum distillation step (VDU2) for separating the reformed oil into various viscosities. The method of claim 1, wherein the method, the lead-sensing lubricator further comprises one or more optionally in the solvent dewaxing step (SDW), hydrofinishing reaction step (HDT) and fractional distillation step (FS). Preparation method. The method of claim 1 or 2, wherein the aromatic extract introduced into the hydrogenation reaction (HT) is a composite aromatic extract (CAE, Composite Aromatic Extract), distillate aromatic extract (DAE, Distillate Aromatic Extract) or glass A method for producing lead-based lube base oil, characterized in that the private aromatic extract (RAE, Residue Aromatic Extract). According to claim 1 or 2, wherein the aromatic extract introduced into the hydrogenation reaction (HT) has a kinematic viscosity of 170 ~ 5,100 centistokes at 40 ℃, specific gravity 0.98 or more, aromatic content is 70% by weight or more Method for producing lead-based lube base oil. The process of claim 1 or 2, wherein the hydrogenation reaction (HT) is performed using a nickel-molybdenum-based (Ni-Mo) catalyst and has a fluid space velocity of 1.0 / hr or less, a pressure of 1,800 psig or more, 350 under hydrogen inflow. A method for producing lead-based lube base oil, characterized in that carried out at a temperature above ℃. The method of claim 1 or 2, wherein the second vacuum distillation step (VDU2) is carried out at a tower static pressure of 70 to 80mmHg, a column top temperature of 70 to 90 ℃ and a column bottom pressure of 135 to 165mmHg, a tower bottom temperature of 300 to 350 ℃ A method for producing lead-based lube base oil. A lead-based lube base oil prepared by the method according to claim 1 or 2, having a kinematic viscosity at 40 ° C. of 6 to 750 centistokes, a specific gravity of 0.876 to 0.934, and a paraffinic hydrocarbon carbon ratio of 55% or less. .

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