DD223163A1 - PROCESS FOR PREPARING AGING-RESISTANT LOW VISCOSES LUBRICATING COMPONENTS WITH VERY HIGH VISCOSITY INDEX - Google Patents

Abstract

The invention relates to a process for the preparation of aging-stable, low-viscosity lubricating oil components with very high viscosity index from Erdoelvakuumdestillaten in a two-stage hydrosolating process with separation of 350 C boiling components after the first stage and separate hydrosolation of the distillation residue in the second stage. According to the invention, the process is carried out such that oil boiling distillates of the boiling point 350 to 530 C in the first stage are treated on a high-hydrogenation cleavage catalyst and in the second stage on cleavage catalysts having reduced hydrogenation activity such that the cleavage rate in each stage is at least 60%.

Description

5. YI. 1983

Title of the invention

'Process for the preparation of aging-resistant low-viscosity lubricating oil components with a very high viscosity index.'

Field of application of the invention

The invention relates to a process for the production of low-viscosity lubricating oil .alterungsbeständigen components with very high viscosity index from Erdölvakummdestillaten the boiling range 350 to 530 ⁰ G by a hydro-catalytic processing ·

Characteristic of the known technical solutions

Lubricating oil components with a very high viscosity index (VI> 120) are obtained in addition to gasoline and diesel fuel in the hydrocracking of petroleum vacuum distillates or deasphalted Vekuumrückständen the petroleum processing from the remaining after separation of 350 ⁰ C boiling fractions residues. The Eydrospaltprozeß is carried out both in one stage with recycling of the residue (recycling) as well as two-stage with separation of boiling to 350 ⁰ G shares between the 1st and 2nd stage.

The hydrosoluble base oils, however, suffer from the disadvantage that they are not stable to aging, i. h ,, that, under the conditions of engine oil aging according to TGL 17 745 (180 ⁰ G,

1β sid., 5 1 Xuft / h, Cu catalyst) centrifuge sludge values of greater than 0.3 Ma., -% are obtained. With that, are the. Hydrospaltgruhdöle. unsuitable for use in multigrade engine oils, turbine oils and. hydraulic oils. To reduce the 'centrifuge sludge values to less than 0.5 Ma .- ^ are elaborate Hachbehandlungsverfahren, such as .z. B ·

j ... - 'Redistillation and / or solvent refining and / or hypofluorination and / or perculation required.

  'i' ...

. Object of the invention

It is an object of the invention to provide a process for the preparation of ^: aging stable, low viscosity lubricating oil compor. ⁰ C to develop components with a high viscosity index by a hydro- catalytic processing of petroleum vacuum distillates boiling range of 350 to 530, which allows ,, to reduce the cost of 'post-processing of these components significantly. ',''

Darl-egung of the essence of the invention

The invention is based on the object, a process for the preparation of aging-stable, .lowly viscous lubricating oil components based on the hydrocatalytic Verar.beiirung Brdölvakuumdestillaten the Siedelage

350 to 530 ^° C., which makes it possible to obtain lubricating oil components with a very high viscosity index and very good aging stability and fuels. The . , "' *

Centrifuge sludge value of the lubricating oil component after aging. (TGL 17 745) should be less than 0.5 Ma.-JS and the vis-> index greater than "120.

was surprisingly found that oil components are obtained with a very high Viskositätsindez und.guter Alterüngsstabilität when in a 'known .. to two-step hydro-cracking process with separation of up to 350 ⁰ C seven' Denden play :: after the first stage and separate hydro-

Cleavage of the distillation residue in the second stage petroleum vacuum distillates of the Siedelage 350 to 530. ' ⁰ G in the first stage of a cleavage catalyst having, high hydrogenation activity, consisting of 1 to 5 wt .-% HiO, 10 to 20 Ma. % HoO-j, 10 to 18 Ma.-SS SiO ₂ as alumosilicate and in the second stage on a cleavage catalyst with increased cleavage activity and truncated hydrogenation activity, consisting of 1 to 6 Ma, -% of an element of VIII. Hebengruppe 'of the Periodic Table , preferably Co or Hi, 10 to 20 M " % of an element of YI. Lifting group of the Periodic Table, preferably W or Mo on a 3 to 40 wt .-% zeolite-containing aluminosilicate with 10 to 18 Ma. % SiO ₂ , at a hydrogen partial pressure of greater than 18 MPa and catalyst loadings of 0.5 to 1.5 v / vh, preferably 0.7 to 1.1 v / vh in the first stage and 0.5 to 2.5 v / vh, preferably 0.9 to 2.0 v / vh, in the final stage and gas to product ratios of 300 to 2500 to 1 nr iH / m, preferably 900 to 1100

3 3

1 m iH / m, in both stages and reaction tempera tures from 390 to 4-60 ⁰ C in the first stage and from 360 to 430 ⁰ C in the second stage are treated, "wherein the cleavage rate at least 60 Ma _a .- % per gap level

The Hydrospaltabstrelfer generated by this method are separately and / or mixed with the Hydrospaltabstreifer the first stage, wherein the proportion of Hydrospaltabstreifers the 2nd stage, at least 30 Ma. -% of the mixture must be freed from the up to 350 ⁰ C boiling fuel shares boiling to 180 ⁰ C • 30 gasoline components are VK components or Reforraereinsätzprodukte. The 180 to 350 ⁰ C boiling diesel fuel fractions have good ignition quality (CZ> 57) and a low BMCI-7 / ert (US Bureau of Mines Correlation Index) of less than 20 and are therefore suitable for the production of lower olefins. The distillation residue with a flash point (M) of greater than 200 ⁰ C.

is with a known solvent mixture, pointed. B, methyl ethyl ketone / toluene, deparaffinized at low temperatures and then bleached with active earths. , The process according to the invention makes it possible to use fuels and / or pyrolysis feedstocks and low viscosity base oil components with very high viscosity indices (greater than 120), and centrifuge Schlain values of less than 0.5 Ma. -% after the Eiichheitsältung (TGL 17 745) produce, the effort compared to the prior art significantly reduced

• 10 becomes,. ',,. _

Another Yorte.il the process of the invention lies in the fact that when re-use of Hydrοspaltruckstandes the 1st stage in the hydrospat process, a lower hydrogen demand, .einen higher Katalj ^ satorbelastung and

-I5 it is possible to use more fission-active catalysts «, ·

The invention will be explained in more detail by two examples. '· .. the. ·'' V. ''''

20 "Example 1,

. ' Sin Yakuumdestillät the Siedelage 350 - 530 ^ with a viscosity at 50 G of 50 mm / s, a Schv / efelgehalt of 1.3 %, a nitrogen content of 1200 ppm and a Ar oma t tight ha It 48% »'of which two and Multikemaromaten 22? S _? is in a first stage at a hydrogen partial pressure of 21.6 IiPa, a flow rate of 1.0 v / vh ,, a mean temperature of 435 ⁰ C and a gas product ratio of 1000: 1 m ^ lH / m on a catalytic ,

Tor ', consisting of 2 % HiO, 15 % MoO., 17 % SiO ₂ and β β % Y-Al ₂ Oo, cleaved. The up; 350 ⁰ C boiling. Fuel, parts are removed by distillation and Destilla'tions-. residue which was based on the Einsätzprodukt in an amount of 35.6 Ma obtained .-%, vrird _v in a second step at a hydrogen partial pressure of 21.6 LTPA, - a rate of '1J5 v / vh, an average temperature from

415 ⁰ C and a gas product ratio of 1000: 1 nri. H./m on a catalyst consisting of β % Co, 11 % WO ,, 5 % zeolite (Z 100), 16% SiO ₂ and 62 % ^ -Al ₂ O ₃ , split · The up to 350 ⁰ C boiling fuel components that make up 60% of the Hydrospaltabstreifers, are removed by distillation and the distillation residue with the one indicated in the table parameters is with a mixture of Hethyl-ethyl-ketone / toluene (60:.. 40 Vol Tl) 'dewaxed at -28 ⁰ C and then hot contacted with 2% bleaching earth at 180 ⁰ C, "the Kennv / erte of the base oil are given in the table.

Example 2

As described in Example 1, "" is a vacuum distillate of Siedelage 350 - 530 ⁰ C in two stages in estate. ' ^: 'Hach standardized hydrogen cleaved the second Kydro-.

cleavage step, the Hydrospaltabstreifer II with the Hydrospaltabstreifer I (1, stage) in the ratio 30: 70 wt .-% mixed 20 and the distillative removal of the boiling to 350 ⁰ C fuel components fed · The obtained Hy. drospaltruckstand, which makes up 40 % of the mixture is, as described in Example 1, worked up to Gruntiöl. The characteristics of the Erado-Spaltrückstandsgemisches and; ; 25 of the base oil made from it are given in the table. '-

table dimension mm / & ÖeiBpiel 1 Hydrosulfate residue II deparaffins u. bleached Example 2 Hydrosoluble residue II / hydrosoluble residue I 30/70 entailed fineness U. bleached > β / -car mg KOH / g Hydrosoluble residue II 0.811. ₍ Hydro- gap - residue II / hydrolytic residue I 30/70 0.813 mm / s Mq .-% 0.808. 11.98 0,810 10.49 Characteristics Ma. -% " 11.28 3.81 10.25 3.45 Γ ^d 50 - 3.73 127.5 3.44 Ι 22 ^V 50 mg / KOH / g 138,5_ neutral '129 0.03 ^V 100 - ° o 0.08 204 0.05 206 VI. ⁰ G 204 -16 206 -20 NZ. ' Ma .-%: ' 0.17 - 0.15 Flpfct * Ma * -% 0.00 - 0.02 - - Stockpkt. Ma .- ^ 0.17 3.5 0.14 4.5 R test - i 1.4445 3.5 1.4451 S content Aging according to TGL 17 745: 1,4426, Air / h, Ou 1.4430 G _A content ^V 50 180 ⁰ G, 16 h, 5 1 12.87 11.44 η ⁷⁰ D HZ ' - 2.1 2.3 R test 0.49 - 0.61 Z Mud - 0.43 - 0.48

Claims (3)

invention claims A process for the preparation of aging stable, low viscosity, very high viscosity index lubricating oil components based on a two step hydrosolating process with separation of the components boiling up to 350G. After the first stage and separate hydrosolation of the distillation residue in the second stage, characterized in that petroleum vacuum distillation - Late the Siedelage 350 to 530 ⁰ C in the first stage of a cleavage catalyst with high hydrogenation activity, consisting of 1 to 5 wt .-% UiO, 10 to 20 Ma, -% MoO ₃ and 10 to 18 Ma .- ^ SiO ₂ as aluminosilicate at catalyst loadings of 0.5 to 1.5 v / vh and in the second, th stage on a cleavage catalyst with increased / cleavage activity and truncated hydrogenation, consisting of 1 to 6 Ma, -% of an element of YIII. Iii group of the periodic table, preferably Co or -.Ui, - 10 to 20 Ma. -% of an element of VI. Periodic table of the Periodic Table, preferably W or Mo, in the form of their oxides on a 3 to 40 Ma. -% zeolite-containing aluminosilicate with 10 to 18 Ma. -% SiO ₂ at Ksitalysatorbelastungen of 0.5 to 2.5 v / vh ,, with hydrogen at a partial pressure of greater than 18.Ii.IPa in both stages and at reaction temperatures of 390 to 460 ⁰ C in the first stage and 360 bis 430 ⁰ C in the. two stage and gas product ratios of 300 to 25OO to 1 ^ iH / m · ⁵ are treated in both stages, the cleavage rate in each stage at least 3Q is 60 % and separating the shares boiling to 350 ⁰ C after the second stage. 2. Method according to point 1, characterized in that the catalyst loading in the first stage is 0.7 to 1, 1 v / vh and in the second stage 0.9 to 2.0 v / vh. Method according to point T and 2, characterized by that the gas product ratio in both stages is ^Λ 900, to 1100 to 1 nri.H / m-. ^v 4. Method according to item 1 to 3, / characterized in that the Hydrospaltabstreifer. the second stage, together with that of the first stage, is freed from the portions boiling to 350 ^° C., the proportion of the second stage hydrospectreaker being at least 30 % of the mixture. .