RU2694054C1 - Method of producing base oil components - Google Patents

Method of producing base oil components Download PDF

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RU2694054C1
RU2694054C1 RU2018130526A RU2018130526A RU2694054C1 RU 2694054 C1 RU2694054 C1 RU 2694054C1 RU 2018130526 A RU2018130526 A RU 2018130526A RU 2018130526 A RU2018130526 A RU 2018130526A RU 2694054 C1 RU2694054 C1 RU 2694054C1
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fractions
hydrocracking
base oils
residue
iii
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RU2018130526A
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Russian (ru)
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Сергей Николаевич Волобоев
Алексей Федорович Мухин
Алексей Михайлович Ткаченко
Роман Евгеньевич Пашкин
Василий Иванович Анисимов
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Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка")
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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen

Abstract

FIELD: chemistry.SUBSTANCE: invention relates to a method of producing high-index components of base oils corresponding to group III and III+ by API, which includes obtaining base oils with viscosity index from 125 to 140. Oil feedstock is subjected to catalytic hydrocracking of petroleum feedstock to obtain non-converted hydrocracker residue, from which by means of vacuum distillation (fractionation) the target fractions are obtained: IB-410 °C, 410–440 °C, 440–480 °C, 480–520 °C, 520 °C – FB and further, after mixing of fractions with paraffin slack wax obtained during solvent dewaxing from raffinates of selective purification of vacuum runs of the primary oil refining process, hydrocracking residue is subjected to successive hydrotreating, catalytic dewaxing (hydroisomerisation), hydrofinishing, carried out at pressure less than 6.0 MPa, rectification and vacuum distillation, with separation of target fraction 370 °C – FB.EFFECT: obtaining a high-index component of base oils with a viscosity index of 120 to 140 points, sulfur content of less than 10 ppm and content of saturated hydrocarbons of not less than 90 wt%, which enables to vary the range in production of commercial oils.1 cl, 27 tbl

Description

The invention relates to a method for producing components of base oils corresponding to group III / III + according to API, and can be applied in the refining industry to obtain components of base oils from unconverted hydrocracking residue, using vacuum distillation (fractionation), catalytic hydrotreating, catalytic dewaxing (hydroisomerization) processes. ), hydrofinishing, rectification and vacuum distillation.

The method allows to obtain components of base oils with kinematic viscosity at 100 ° C from 3.5 mm 2 / s to 8.5 mm 2 / s, viscosity index more than 120 points, sulfur content less than 10 ppm (0.0010% wt.) And the content of saturated hydrocarbons is not less than 90% wt.

From the literature it is known that the production technology of the components of base oils may include:

- or a number of physico-chemical methods for cleaning raw materials from undesirable components, including the processes of selective cleaning and dewaxing;

- or a set of catalytic hydrofining processes (hydrocracking, hydrogenation, hydroisomerization, hydrodewaxing);

- or the combination of one or more hydroprocesses with physico-chemical methods.

The main disadvantage when using for the production of high-index base oils only physico-chemical cleaning methods is the low yield of the target product to 50% wt. for raw materials. The combination of hydroprocesses with physicochemical purification methods makes it possible to achieve the necessary purification of an oil feedstock with selective solvents to obtain components of base oils of the required quality and a higher yield of the target product.

The use of a set of several processes of catalytic hydrofining, including hydroisomerization, hydrodewaxing, requires a significant consumption of hydrogen-containing gas, the use of expensive equipment, which allows to conduct processes at pressures above 10.0 MPa, imported catalytic systems.

Despite the fact that a wide variety of technological schemes, operating conditions and catalysts are used in the industrial production of base oils, there remains a need for new methods, including methods for using heavy hydrocracking fuel that can reduce costs and improve work efficiency.

A method of obtaining oils by hydrofining and dewaxing oil fractions after selective purification, followed by vacuum distillation of the dewaxed product to obtain distillate and residual components of different viscosity [Zolotnikov V.Z. and others. Hydrogenation upgrading of crude oil to improve the technology of production of lubricating oils. Thematic review. Series: Oil refining. - M .; TsNIITEneftekhim, 1986, p. 47-48.].

A method of obtaining the basic components of petroleum oils by hydrocracking straight-run vacuum distillate, with the release of the residual hydrocracking fraction, which is partially sent for recycling to the raw materials of the process in an amount of from 0.5 to 60% wt. on the raw materials of the process [RU 2109793]. The change in the amount of residual fraction of hydrocracking recycling regulates the increase in the temperature of the boiling end of the feed stream to 480-520 ° C and the yield of the light and heavy fractions obtained by fractionation of the balance part of the residue. Light and heavy fractions are sent to the dewaxing selective solvent (MEK / toluene). Dewaxed oil is subjected to purification of clay.

The method allows to obtain base oils with kinematic viscosity at 100 ° С from 3.1 to 5.5 mm / s, with a viscosity index of more than 125 points.

The disadvantage of this method is a decrease in the productivity of the hydrocracking unit due to the use of recycling to increase the conversion rate of (undesirable) polycyclic aromatic hydrocarbons. Tertiary treatment with clay is not an environmentally friendly process due to the inability to regenerate the main component of the process - clay.

A method of obtaining base oils from the residue of hydrocracking of crude oil using solvent extraction processes (phenol), dewaxing (MEKUMIBK), followed by fractionation with separation of the target fraction sent to hydrotreating [US 2004245147]. A base oil is obtained with a viscosity index of up to 117 points, a kinematic viscosity at 100 ° C, 7.05 mm / s, and a pour point of minus 12 ° C.

The disadvantage of this method is to obtain one target narrow fraction with a low yield. The resulting base oil product in terms of viscosity index does not meet the specifications set by the American Petroleum Institute (API) for Group III base oils.

A method of obtaining lubricating base oil of low kinematic viscosity with a high viscosity index by hydrocracking of crude oil with the release of the residue of hydrocracking, followed by its dewaxing and hydrotreating [US 5460713]. As a raw material for hydrocracking, a mixture of not only vacuum gas oil and coking gas oil is used, but also ga is a paraffin product of the process of dewaxing distillate raffinates. Base oil is obtained with a viscosity index of more than 120 points, kinematic viscosity at 100 ° C from 3.0 to 7.5 mm / s with a pour point of minus 10 ° C.

The disadvantages of this method include obtaining one broad fraction of the base oil.

A method of obtaining lubricating base oil with a high viscosity index and low kinematic viscosity by hydrocracking of crude oil (a mixture of vacuum gas oil and coking gas oil) with the release of the residue of hydrocracking followed by its dewaxing and hydrotreating [US 5462650].

The method allows to obtain a base oil with a kinematic viscosity of 3 to 5 mm 2 / s, a viscosity index of at least 120 points, and a pour point of minus 10 ° C.

Mixed raw materials of hydrocracking refers to the classic version of a mixture of vacuum gas oil and gas oil coking, the upper limit of the boiling point of which does not exceed 480 ° C.

Closest to the proposed method is a method of obtaining high-quality base oil using catalytic processes of hydrocracking, hydrodewaxing (improving low-temperature performance by changing the structure of long-chain paraffins) and hydrofining (color improvement, stability) [US 5358627].

The method allows to obtain a base oil after distillation with a viscosity index in the range of 95-100 points.

The disadvantage of this method is the low viscosity index.

The aim of the proposed technical solution of the invention is to develop a method for producing high-index components of base oils corresponding to group III and III + according to API, using as raw material the unconverted residue of hydrocracking of the fuel direction in a mixture with paraffin sludge obtained in the process of solvent dewaxing from vacuum refined refined refineries epilogues (hereinafter referred to as i / p) of the process of primary oil refining (AVT) and from the unconverted hydrocracking residue according to the technological scheme by applying hydrofining processes, catalytic isodewaxing, hydrofinishing, carried out at a pressure below 6.0 MPa and, at the final stage, rectification and vacuum distillation.

This goal is achieved using hydrocracking units as raw materials along with straight-run raw materials - vacuum gas oil, and secondary products: coking gas oil, residual extract - a by-product of selective purification, in an amount of 4 to 6% by weight, and petrolatum - a by-product of dewaxing residual raffinate , in an amount of from 1 to 3% wt. This allows you to get hydrofluorine unconverted hydrocracking residue containing at least 90% wt. saturated hydrocarbons, including isoparaffin hydrocarbons of at least 30% wt. and a viscosity index of more than 120 points, which is a high-quality raw material for the production of high-index oil components.

Next, the unconverted hydrocracking residue is sequentially subjected to: vacuum distillation (fractionation), in order to isolate the target fractions: HK-410 ° C, 410-440 ° C, 440-480 ° C, 480-520 ° C, 520 ° C - KK; Further, the fractions, depending on the desired viscosity, individually or mixed with each other in any ratio, are mixed with paraffin gum, obtained in installations of solvent dewaxing of raffinate oils for selective purification of vacuum fractions of the primary oil refining process (AVT) and / or from untransformed hydrocracking residue, in the ratio: paraffin slack - no more than 90%; fractions (mixture of fractions) of the unconverted hydrocracking residue — up to 100% and successively undergo: hydrotreatment, in order to saturate unsaturated hydrocarbons and remove sulfur compounds, nitrogen and dyes, then catalytic dewaxing (hydroisomerization) - in order to lower the freezing temperature to no higher than minus 15 ° C; then hydrofinishing - to saturate olefins, residual aromatics and to remove coloring substances in the dewaxed product. At the final stage, by distillation and vacuum distillation, components of base oils with a kinematic viscosity at 100 ° C are separated: 3.5-4.0 mm 2 / s; 4.0-4.5 mm 2 / s; 4.5-5.5 mm 2 / s; 5.5-6.5 mm 2 / s; 6.5-7.5 mm 2 / s; 7.5-8.5 mm 2 / s.

The implementation of the invention:

Hydrocarbon feedstock, which includes straight-run vacuum gas oil obtained from a mixture of low-sulfur oils, heavy coking gas oil, as well as by-products of secondary solvent processes - residual extract of selective deasphalt refining in an amount of from 4 to 6% by weight. and petrolatum - the product of dewaxing the residual raffinate in an amount of from 1 to 3% by weight, passes the following stages of processing:

a) hydrocracking of mixed hydrocarbon feedstock at a pressure of at least 13.5 MPa, temperature from 380 ° C to 430 ° C, volumetric feed rate of the feedstock from 0.5 to 1.5 h -1 with a degree of conversion of at least 75% with the release of unconverted the residue of hydrocracking containing at least 90% wt. saturated hydrocarbons, including isoparaffin hydrocarbons of at least 30% wt;

b) vacuum distillation (fractionation) of the unconverted hydrocracking residue at a temperature in the column (top / bottom) 82 ° C / 235 ° C and pressure (top / bottom) 0.005 MPa / 0.01 MPa with the release of the desired fractions: NC-410 ° C , 410-440 ° С, 440-480 ° С, 480-520 ° С, 520 ° С - КК;

c) mixing the fraction (mixture of fractions) of the unconverted residue obtained in stage b) with paraffin sod at a temperature not higher than 90 ° C in the ratio: acac paraffin - not more than 90%; fraction (mixture of fractions) of unconverted hydrocracking residue - up to 100%. Depending on the fraction used (mixture of fractions), as well as by changing the amount of Gacha involved and the type of Gacha (gauch from II v / p, III v / p, IV v / p, unconverted residue), the resulting kinematic viscosity is adjusted at 100 ° С oils: 3.5-4.0 mm 2 / s; 4.0-4.5 mm 2 / s; 4.5-5.5 mm 2 / s; 5.5-6.5 mm 2 / s; 6.5-7.5 mm 2 / s 7.5 mm 2 / s - 8.5 mm 2 / s, as well as the viscosity index of the base oil: from 120 to 140 points;

d) Hydrotreating a mixture of the fraction (mixture of fractions) of the unconverted hydrocracking residue with paraffin slack obtained in stage c) in the presence of a catalyst containing at least one of the metals VI and VIII of the periodic table of chemical elements, at a temperature of 300 to 400 ° C, pressure from 3.5 to 6.0 MPa, with a bulk feed rate from 0.5 to 1.50 h -1 and circulation ratio from 500 to 1100 nm 3 / m 3 of hydrogen-containing gas;

d) hydrodewaxing (hydroisomerization) of the hydrotreated mixture of the fraction (mixture of fractions) of the unconverted hydrocracking residue with slack obtained in step d) in the presence of a catalyst containing at least one of the metals of the VIII group of the periodic table of chemical elements at a temperature from 290 to 400 ° C, pressure from 3.5 to 6.0 MPa, with a bulk feed rate from 0.5 to 1.50 h -1 and circulation ratio from 1200 to 3800 nm / m of hydrogen-containing gas;

e) hydrofinishing of a hydrotreated dewaxed mixture of a fraction (mixture of fractions) of the unconverted hydrocracking residue with slack obtained in step d), in the presence of a catalyst containing at least one of the metals of group VIII of the periodic table of chemical elements, at a temperature of from 180 to 300 ° C , pressure from 3.5 to 5.3 MPa, with a bulk feed rate from 0.5 to 1.50 h -1 and circulation ratio from 1200 to 3800 nm 3 / m 3 of hydrogen-containing gas;

g) rectification, at a temperature in the cube of the distillation column not more than 330 ° C and pressure not more than 0.17 MPa, hydroformed mixture of the fraction (mixture of fractions) of the unconverted hydrocracking residue and slack obtained in stage e), with the release of the fraction NC-280 ° C, later used as a component of commercial fuels, and a fraction of 280 ° C — KK.

h) Vacuum distillation, at a temperature in the bottom of the vacuum column not exceeding 315 ° C and abs pressure. not more than 0.05 MPa, fractions 280 ° С - KK, obtained from the hydroformed mixture of the fraction (mixture of fractions) of the unconverted hydrocracking residue with slack at the stage g), with separation of the fractions 280 ° С - 370 ° С, sent as a component to the commercial fuels, and fractions of 370 ° C - KK - a high index component of base oils.

The raw mixed feedstock is subjected to catalytic hydrocracking, with a pressure of at least 13.5 MPa, a temperature of 380 ° C to 430 ° C, a space feed rate of 0.5 to 1.5 h -1 and a conversion of at least 75%.

Table 1 shows typical physico-chemical characteristics of the unconverted hydrocracking residue with a mass fraction of sulfur of less than 30 ppm (0.0030% by mass), namely, 0.0024% by mass, and a saturated hydrocarbon content of not less than 90% by mass, including isoparaffin hydrocarbons not less than 30 wt.%, which is promising, in terms of its use as a raw material, for the production of high-index components of base oils of groups II and III according to API classification.

Figure 00000001

Figure 00000002

The resulting unconverted hydrocracking residue containing at least 90% wt. saturated hydrocarbons, including isoparaffin hydrocarbons of at least 30% wt, are subjected to vacuum distillation (fractionation) in order to obtain the target fractions: NC - 410 ° C, 410-440 ° C, 440-480 ° C, 480-520 ° C, 520 ° С - КК, at a temperature in the column (top / bottom) 82 ° С / 235 ° С and pressure (top / bottom) 0.005 MPa / 0.01 MPa. Tables 2, 3 show typical physico-chemical characteristics of the fractions.

Figure 00000003

Figure 00000004

Obtained target fractions of the unconverted hydrocracking residue after accumulation, alternately, depending on the required viscosity, separately or mixed with each other in any ratio, are mixed with paraffin slack obtained on the solvent dewaxing installations of raffinate oils for the selective purification of vacuum chases of the primary processing oil (AVT); from untransformed hydrocracking residue, in the ratio: paraffin slack - no more than 90%; unconverted hydrocracking residue - up to 100%.

Table 4 shows the typical characteristics of paraffin gachi according to the SR PR 029-00148599-2011

Figure 00000005

Figure 00000006

The essence of the invention will be shown on the example of the mixing of the NK fractions - 410 ° C, 410-440 ° C, 440-480 ° C, 480-520 ° C of the unconverted hydrocracking residue with mixed tar in ratios: 30:70, 50:50, 70: thirty.

Tables 5.6 show the physico-chemical characteristics of the resulting mixture of NK fractions - 410 ° C, 410-440 ° C, 440-480 ° C, 480-520 ° C of the untreated hydrocracking residue with hachech.

Figure 00000007

Figure 00000008

Figure 00000009

The resulting mixture is subjected to Hydrotreating in the presence of a catalyst containing at least one of the metals of the VI and VIII groups of the periodic table of chemical elements at a temperature of from 300 to 400 ° C, a pressure of 3.5 to 6.0 MPa, with a volumetric feed rate raw materials from 0.5 to 1.50 h -1 and circulation ratio from 500 to 1100 nm 3 / m 3 of hydrogen-containing gas.

Table 7 shows the physico-chemical characteristics of the hydrotreated NK mixtures - 410 ° C, 410-440 ° C of the unconverted hydrocracking residue and slack. Hydrotreating was carried out with the following process parameters: volumetric rate V = 1.5 h -1 ; pressure P = 5.0 MPa; temperature T = 320 ° C; the multiplicity of circulation of VSG / raw materials = 600 nm / m.

Figure 00000010

Figure 00000011

Table 8 shows the physico-chemical characteristics of hydrotreated mixtures of 440-480 ° C, 480-520 ° C of the unconverted residue of hydrocracking with scab. Hydrotreating was carried out with the following process parameters: volumetric rate V = 1.5 h -1 ; pressure P = 5.0 MPa; temperature T = 340 ° C; the multiplicity of circulation of VSG / raw materials = 600 nm 3 / m 3 .

Figure 00000012

Next, the hydrotreated mixture of the fraction of the unconverted hydrocracking residue with gadget undergoes a catalytic dewaxing (hydroisomerization) in the presence of a catalyst containing at least one of the metals of group VIII of the periodic table of chemical elements, at a temperature of from 290 to 400 ° C, pressure from 3.5 up to 6.0 MPa, with a bulk feed rate from 0.5 to 1.50 h -1 and a multiplicity of circulation of hydrogen-containing gas from 1200 to 3800 nm 3 / m 3 and hydrofinishing in the presence of a catalyst containing at least one of the metals Group VIII Periodic table of chemical elements, at a temperature of from 180 to 300 ° C, a pressure of 3.5 to 6.0 MPa, with a bulk feed rate of 0.5 to 1.50 h -1 and a circulation ratio of 1200 to 3800 nm 3 / m 3 of hydrogen-containing gas.

Tables 9–20 show the characteristics of hydrotreated mixtures of the target fractions of the unconverted hydrocracking residue with gaut after catalytic dewaxing (hydroisomerization) and hydrofinishing.

Figure 00000013

Figure 00000014

Figure 00000015

Figure 00000016

Figure 00000017

Figure 00000018

Figure 00000019

Figure 00000020

Figure 00000021

Figure 00000022

Figure 00000023

Figure 00000024

Figure 00000025

Figure 00000026

Figure 00000027

Figure 00000028

Figure 00000029

Next, the resulting hydrofluorine mixture of the fraction of the unconverted hydrocracking residue with ganch undergoes rectification and vacuum distillation, with the separation of the 370 ° C fraction — KK — component of base oils.

The material balances of the distillation of a hydrofluorised mixture of the target fractions of the unconverted hydrocracking residue and hacc are given in Table No. 21-24.

Figure 00000030

Figure 00000031

Figure 00000032

Figure 00000033

Figure 00000034

Figure 00000035

Tables 25, 26 show the quality indicators of the target fraction of 370 ° C - QC obtained from hydrofluorised mixtures of fractions of the unconverted hydrocracking residue with pruphinic slack at various ratios and modes of catalytic dewaxing (hydroisomerization) and hydrofinishing

Figure 00000036

Figure 00000037

Figure 00000038

Figure 00000039

Table 27 lists the API classification requirements for base oils.

Figure 00000040

Analysis of the data presented in tables 25, 26 and 27 shows that the viscosity index of the obtained components of base oils with different modes of catalytic dewaxing (hydroisomerization) and hydrofinishing processes ranged from 125 to 140 points, the content of saturated compounds is not less than 90.0% by weight , sulfur - less than 10 ppm (0.0010% wt), which meets the requirements for the quality of base oils of III and III + groups according to API.

EFFECT: obtaining high-index components of base oils from fractions of unconverted hydrocracking residue that meets the requirements for oils of the III and III + groups according to API, with pressure of conducting hydroprocesses less than 6.0 MPa. The production of high-index base oils with a high level of saturated compounds provides an improvement in the performance characteristics of commercial oils, which is not achieved by the use of new multifunctional additives or by the thickening of oils.

Claims (1)

  1. The method of obtaining high-index components of base oils of groups III and III + by API, characterized in that to obtain base oils with a viscosity index from 125 to 140, the crude feedstock is subjected to catalytic hydrocracking of crude oil, to produce an unconverted hydrocracking residue, from which using vacuum distillation (fractionation ) get the target fractions: NC - 410 ° C, 410-440 ° C, 440-480 ° C, 480-520 ° C, 520 ° C - KK and further, after mixing the fractions with paraffin slack, obtained in the process of solvent dewaxing from refined with selective purification of vacuum cuts of the process of primary oil refining, the hydrocracking residue, is sequentially subjected to: hydrotreatment, catalytic dewaxing (hydroisomerization), hydrofinishing, carried out at a pressure less than 6.0 MPa, rectification and vacuum distillation, with the release of the target fraction 370 ° C - QC.
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5358627A (en) * 1992-01-31 1994-10-25 Union Oil Company Of California Hydroprocessing for producing lubricating oil base stocks
US5460713A (en) * 1992-10-02 1995-10-24 Mitsubishi Oil Co., Ltd. Process for producing low viscosity lubricating base oil having high viscosity index
US8834706B2 (en) * 2010-06-04 2014-09-16 Sk Innovation Co., Ltd. Method for preparing lubricating base oils by using vacuum distilled deasphalted oil
WO2016166293A1 (en) * 2015-04-15 2016-10-20 Neste Corporation A method for producing oil-based components
RU2604070C1 (en) * 2015-08-20 2016-12-10 Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка") Method of producing high-index components of base oils
RU2649395C1 (en) * 2017-07-24 2018-04-03 Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка") Method of high-index components of base oils preparation

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5358627A (en) * 1992-01-31 1994-10-25 Union Oil Company Of California Hydroprocessing for producing lubricating oil base stocks
US5460713A (en) * 1992-10-02 1995-10-24 Mitsubishi Oil Co., Ltd. Process for producing low viscosity lubricating base oil having high viscosity index
US8834706B2 (en) * 2010-06-04 2014-09-16 Sk Innovation Co., Ltd. Method for preparing lubricating base oils by using vacuum distilled deasphalted oil
WO2016166293A1 (en) * 2015-04-15 2016-10-20 Neste Corporation A method for producing oil-based components
RU2604070C1 (en) * 2015-08-20 2016-12-10 Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка") Method of producing high-index components of base oils
RU2649395C1 (en) * 2017-07-24 2018-04-03 Общество с ограниченной ответственностью "ЛУКОЙЛ-Волгограднефтепереработка" (ООО "ЛУКОЙЛ-Волгограднефтепереработка") Method of high-index components of base oils preparation

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