DE2110576C2 - Process for the production of lubricating oil with a high viscosity index - Google Patents

Description

30th

From US-PS 34 93 493 is a process for the production of lubricating oils with a high viscosity index known, in which, for example, a high-boiling "wlineral oil fraction of the type of a deasphalted Residual oil hydrocracked in the presence of a catalyst. which is a metal oxide or metal sulfide of e.g. B. Nickel as well as molybdenum or tungsten and optionally also a halogen, such as fluorine, on an aluminum oxide carrier contains. The total content of active metals should expediently be at least 20% by weight and preferably at least 30% by weight, based on the total analyzer.

Surprisingly catfish has now been found that special favorable results with regard to the viscosity index achievable in the end product can be obtained, even when using a very low viscosity index feed when using a catalyst which contains certain amounts of phosphorus.

The inventive method for producing a lubricating oil with a high viscosity index by hydrocracking a high-boiling mineral oil fraction at elevated pressure and elevated temperature in the presence of a catalyst composed of 3 to 16 wt .-%, nickel, 6 to 24 wt .-% molybdenum or tungsten, each In metallic, oxidic or sulphidic form and optionally 1 to wt .-% fluorine on a refractory oxide support, is accordingly characterized in that the catalyst used also contains 1 to 12 wt .-% phosphorus, calculated as P1O5 that is below a temperature abdestllllen of 350 to 400 ° C boiling fractions of the hydro- ⁶ "cracked product and entparafflniert the lubricating oil residue and that, if appropriate, the soft paraffin obtained in the dewaxing in the presence of a wasserstoffhaltlgen gas catalytically slomerlslert and entparafflniert the Hydrolsomerlsat for preparing a lubricating oil with a very high viscosity index .

Starting materials suitable for the process according to the invention are high-boiling hydrocarbon mixtures, e.g. B. heavy petroleum fractions obtained by pyrolysis of coal, coal shale or tar sand. Petroleum fractions which at least partially boil above the boiling range of lubricating oil can be used with advantage. The feed material used for the process according to the invention is preferably a distillate fraction which has been obtained by vacuum distillation from a residual oil fraction obtained by distillation at atmospheric pressure. The boiling range of such a vacuum distillate is generally between 350 and 550 ⁰ C., deasphalted residual oil fractions are, however, particularly preferred.

Pure hydrogen can be used in the process according to the invention, but this is not essential necessary. A gas with a hydrogen content of 70% by volume or more is excellent. In practice it is preferred to use a hydrogen-containing gas obtained from a catalytic reformer originates. Such a gas not only has a high hydrogen content, but also contains low boiling points Hydrocarbons such as methane and a small amount of propane.

The temperature and pressure used in the process of the invention can vary depending on the desired degree of conversion vary within wide limits. Suitably the chosen temperature is not below 350 ° C and not above 500 ° C. At temperatures below 350 ° C the degree of conversion is reduced, while at temperatures above 550 ° C cracking occurs to such an extent that only limited cracking occurs Amount of the desired product is obtained. A temperature between 400 and 500 ° C is preferred. Pressures below 50 bar are less desirable because they reduce the life of the catalyst while at the same time there is a risk of an excessively high aromatic content in the product, which makes the viscosity index disadvantageous being affected. A pressure above 250 bar would require very expensive equipment. Preferred catfish a pressure between 100 and 200 bar is used.

The hourly liquid space flow velocity and the hydrogen / oil ratio are similarly chosen within very wide limits. However, an hourly liquid space flow rate is preferred between 0.1 and 10 kg of oil / hour / liter of catalyst is used. An hourly Liquid space velocity less than 0.1 kg / hr / L would be for a given catalyst Conversion rates require an inefficiently large reactor while an hourly liquid space flow rate of more than 10 kg / h / l catalyst would result in only a low degree of conversion to the desired product. The hydrogen / oil ratio is preferably 100 to 5000 liters (at 1 bar and 0 ° C.) per kg of oil. A very low Hj / oil ratio would adversely affect the life of the catalyst while having a very high Hj / oil ratio would cause a considerable pressure drop over the catalyst bed, so that a lot of energy for the Compression would be required to recycle the hydrogen rich gas.

A catalyst is preferred in the context of the invention used. In which the atomic ratio of nickel to molybdenum or tungsten is below 0.75: 1 and In particular in the range of 0.2: 1 and 0.65: 1. The best results are achieved with the Nl / Mo combination.

When using such catalysts, the According to the invention production of lubricating oil preferably at a temperature of 375 to 425 ° C, a Pressure from 100 to 200 bar, a space flow rate of 0.5 to 1.5 kg of feed per liter Catalyst per hour and a hydrogen / loading ratio carried out from 500 to 2500 liters of hydrogen / kg of feed.

In addition, a phosphorus content is particularly preferred of the catalyst between 2 and 9 wt. Sb, calculated as P2O5 in relation to the total catalyst, and es it was found that the maximum activity of the catalyst at a phosphorus content between 3 and 7 Weight-5b, calculated as PjO * in relation to the total catalyst, is achieved.

In the context of the invention, "activity" is to be understood as the temperature which is required to _{obtain a product with a predetermined viscosity index under the given operating conditions (pressure, hourly liquid space flow rate, H 2} / oil ratio) and based on a given charge . The higher the activity of the catalyst used, the lower the temperature required will be.

In principle, any refractory material can be used as a support for the catalyst to be used. Suitable materials are, for example, aluminum oxide, silicon oxide, magnesium oxide, titanium oxide, zinc oxide, Thorium oxide, boron oxide and mixtures and compounds of these metal oxides.

The use of aluminum oxide or a mixture of silicon oxide and magnesium oxide as a carrier material enables the production of ve.- catalysts with particularly good activity, selectivity and stability.

Commercial aluminum oxide generally contains small amounts of impurities, especially Silicon oxide and sodium. It has been found that aluminum oxide containing 0.5 to 3 wt Silica and up to 0.005 wt% sodium, an excellent one Support material for the catalyst is, which is why this aluminum oxide is preferred.

If the alumina contains more than 0.005 wt% sodium, the sodium content can be ion-exchanged be reduced to the desired value with a solution of an ammonium salt.

Of the carriers, which consist of silicon oxide and magnesium oxide, a mixture of 50 to 90 Wt% silica and 10 to 50 wt% magnesia preferred.

Under the selectivity of a catalyst is under of the invention to understand the yield of lubricating oil with a certain viscosity index, which under given conditions (temperature, pressure, hourly liquid space flow velocity and Hj / oil ratio) was obtained with the aid of the particular catalyst. The stability of the catalyst is the extent up to which the catalyst its activity during prolonged use in the invention Procedure maintains.

In order to increase the activity and selectivity of the catalyst even further, it is advisable to use Fluorine In added to the specified quantities.

The catalyst can be made in any desired manner be done by, for example, the carrier with one or more aqueous solutions of compounds the other components are impregnated and then dried and calcined. When the impregnation If it is carried out in several stages, the material can, if desired, be between successive ones Impregnation stages are dried and calcined.

Catalysts with particularly good activity, stability and selectivity can be prepared by a Impregnation is carried out with an aqueous solution that contains both a phosphomolybdate and a nickel salt, instead of two separate solutions, one of which is phosphoric acid and the other is molybdate and contains a nickel salt.

Nickel hexamine dichloride [Ni (NHj) ₆ ] _{Cl 2} or nickel formate is preferably used as the nickel salt.

To ensure that the nickel salt, the phosphomolybdate and / or the acidic phosphomolybdate during the impregnation on the catalyst thoroughly If dispersed, it is preferred to the solutions add ammonium hydroxide to these components, the amount of which is such that the pH value of these solutions is between 7 and 12.

Between successive impregnations (e.g. 3 to 10) and after the last impregnation the kataiysalor dried. The drying is preferably 0.5 to 5 hours at a temperature between 100 and 250 ° C.

For the additional storage of fluorine, the catalyst is preferred with a solution of hydrogen fluoride, Ammonium fluoride and / or ammonium fluoride impregnated. These components have the advantage that they do not have any less desirable cations, such as Na, K, and Ca ions, on the catalyst after calcination leave behind.

The preparation of the catalyst is done by calcining completed. This treatment is preferably carried out at a temperature between 450 and 850 ° C for 0.5 carried out up to 5 hours.

After calcining, phosphorus and the metals, namely nickel and molybdenum or tungsten, are in the catalyst presumably present in the form of oxides, although the possibility that they may not be excluded have at least partially connected to the catalyst.

It has been found that in the catalytic overrun of mixtures of heavy hydrocarbons Better results can be achieved in lubricating oil by means of hydrogen if the catalyst sulphidated beforehand is, so that the metal oxides are at least partially converted into the corresponding metal sulfides.

A particularly good and therefore preferred sulfide

method is to use the catalyst at a Temperature between 250 and 450 ° C, a pressure between 30 and 70 bar, an hourly space flow velocity between 1 and 10 kg oil / h / l catalyst and a hydrogen / oil ratio between 50 and 500 liters of Hi / kg of oil with a sulfur compound

containing oil, preferably with a gas oil, in contact. This treatment is preferred Carried out in the same reaction vessel in which the hydrocracking takes place. The lubricating oil residue separated by distillation from the hydrocracked product generally contains Paraffins that solidify at a slightly reduced temperature and therefore reach the pour point of the desired Lubricating oil have an adverse influence. A useful lubricating oil or lubricating oil component to produce from the residue, this is dewaxed and the soft paraffin is separated off. This treatment can be carried out in any desired catfish. Preference will be given to the

paraffinic with the help of a mixture of methyl ethyl ketone and toluene at a temperature between -10 and -40 ° C and a volume ratio of solvent to oil between 1: 1 and 10: 1 carried out.

The dewaxed residue has a high viscosity index, for example a viscosity index between 100 and 140, depending on the conditions under which the hydrogenating conversion of the starting material has taken place.

For this reason it is for use as a multigrade lubricant oil or as a multigrade lubricant oil component extremely suitable. In addition, this dewaxed residue allows the production of an or several lubricating oils or lubricating oil components with high viscosity indices and different from one another Viscosities by vacuum distillation, these oils or components in turn being excellent Mefer lubricating oils can be reconditioned, by mixing them with other components.

According to a preferred embodiment of the invention The soft paraffin obtained in the dewaxing treatment is erstoffhaltigen in the presence of eices ^ Catalytically isomerized gas. This hydromeration is preferably carried out under the following conditions:

temperature 310 to 450 ° C pressure 50 to 200 bar Room flow 0.1 to 5.0 liters of soft paraffin speed per hour / l catalyst Hydrogen/ 100 to 5000 IH ₂ Soft paraffin (under normal pressure and relationship normal temperature) per kg What paraffin.

The catalyst used in the hydroisomerization zone contains a component having hydrogenation activity and having an acidic solid refractory support is combined with isomerization activity.

The amount of the hydrogenation component can vary within wide limits, advantageously between 0.5 and 40% by weight, calculated on the total catalyst, with the remainder consisting of the solid, acidic, refractory support consists.

The hydrogenation component of the catalyst preferably contains one or more metals from groups Ib, Hb, Va, Via, VIIa and / or VIII of the periodic System of the elements and / or one or more oxides and / or sulfides of one or more of these Metals.

A sulfur-resistant catalyst is preferably used in the Hydroisor.wrlslerungszone. Particularly a.Htlve sulfur-resistant catalysts contain one or more oxides and / or sulfides of group VIa (Cr, Mo, W) and / or the elsenic group (Fe, Ni, Co). A very preferred catalyst for hydroisomerization contains 6 to 24 wt .-% tungsten and / or molybdenum and 3 to 18 wt .-% nickel and / or cobalt In the Shape of your oxides and / or sulfides.

The acidic refractory support of the catalyst to be used in the hydroisomerization zone preferably contains a mixture and / or a compound of silicon oxide and aluminum oxide, of aluminum oxide and BF], of silicon oxide and magnesium oxide, of silicon oxide, aluminum oxide and zinc oxide, or of aluminum oxide and P2O5. Acid treated clays and zeolitic crystalline molecular sieves are also very suitable for this purpose. In order to increase the activity of the catalyst, fluorine is preferably added to the carrier in an amount of 1 to 6 Qev /.-% , whereby its acldity is increased.

The most preferred catalyst for hydro

Isomerization zone contains 3 to 18% by weight of nickel, 6 up to 24% by weight molybdenum, 1 to 6% by weight fluorine and 2 to 9% by weight of PiOs deposited on a carrier which consists entirely or mainly of aluminum oxide.

If both the product that leaves the Hydrocrackzor.e, and the hydrogen-containing gas one very may have a low sulfur content in the hydroisomerization zone but also a sulfur-sensitive catalyst can be used. When using a such a catalyst can result in a higher yield of lubricating oil, calculated on the basis of the soft paraffin starting material, can be obtained. A common sulfur-sensitive catalyst contains platinum an alumina carrier whose acidity is achieved by the incorporation of chlorine or fluorine (the latter is preferred) was increased.

The hydroisomerization conversion is general not completely who.A it is done in a single operation. The unconverted becomes therefor Soft paraffin removed from the oil obtained in the hydroisomerization by dewaxing.

The effluent from the hydroisomerization zone may contain small amounts of product which are below the Boiling range of lubricating oil, since cracking occurs to a small extent in this zone. To this low boiling point Avoiding components in the oil / soft paraffin mixture to be dewaxed will help Feed to the second dewaxing zone therefore preferably through that portion of the hydroisomerization effluent which boils within the boiling range of lubricating oil.

Under the designation "Hydrocarbons that boil in the boiling range of the lubricating oil" are high-boiling "' To understand hydrocarbons with a viscosity that makes them suitable as lubricating oil components. Although certain lubricating oils can have greater volatility, the majority of lubricating oils have an initial boiling point of at least 350 ° C at atmospheric pressure.

The separation of the hydrocarbons below the boiling range of lubricating oil, from the hydrolsomerization effluent takes place by functioning distillation or flash evaporation.

The dewaxing of the lubricating oil in the boiling area boiling portion from the hydrolsomerization effluent can be carried out in any conventional catfish, conveniently by means of a solvent such as liquid propane, benzene, toluene, methyl ethyl ketone and mixtures of Methyl ethyl ketone and one or more aromatics.

The soft paraffin obtained in the second dewaxing treatment is advantageously used in Recirculated hydroisomerization zone.

The dewaxed oil has a very high viscosity index, namely, depending on the Hydroisomerlsierungsbedlngungen, 'τι range from 140 to 170. It can therefore Excellent as a multi-calf lubricant oil or as multi-calf lubricant oil be used.

The dewaxed residue can also get through Vacuum distillation in a variety of lubricating oils or lubricating oil components with very high viscosity indices and different viscosities are separated from one another. These lubricating oil components can Can be used for the production of excellent multi-calf smelter oils by dividing them among themselves

or mixed with other lubricating oil components. To simplify the process, the Hydrocracking treatment and hydrolsomerisailon advantageously in the presence of the same catalyst carried out.

This catalyst can be contained in two reactors The hydrocracking is carried out in the first reactor and the hydrolsomerization in the second reactor will.

But it is also possible, the hydrocracking and the Hydrolsomarlslerung to be carried out in the same reaction vessel. Only one will grow on this catfish Reactor needed and achieved a considerable improvement in the economics of the process.

If the hydrocracking treatment and the hydrolysis take place in the same Raktlon container, will the soft paraffin separated from the hydroisomer solution product preferably together with the high-boiling paraffin. M! Ncr =! Ö! Frskiion of a combined! Subjected to hydroisomerization / hydrocracking treatment.

The invention is illustrated by the following examples explained in more detail.

Execution bracket I I) Manufacture of heavy-duty hydrocracking Hydrocarbon oils In lubricating oil with a high Viscosity index used catalysts Catalyst A:

250 g of particles obtained by extrusion, which have a diameter of 1.3 mm and consist of aluminum oxide, are treated for 20 hours at a temperature of 22 ° C with a solution of 15.5 cm 'of 85% phosphoric acid (H ₁ PO ₁ ) Impregnated in 241.5 cm ^{1 of} water.

The impregnated carrier is then dried for 2 hours.

A solution of 93 g of ammonium paramolybdate in 270 cm ^{1 of} water is then mixed with a solution of 118 g of sodium hexamine dichloride in a mixture of 160 cm of water and 11 cm of 27% ammonium hydroxide.

The dried catalyst support is impregnated three times for 10 minutes at a temperature of 22 ° C. with the above-described solution of ammonium paramolybdate, nickel hexamine chloride and ammonium hydroxide, the support being dried for 2 hours at 200 ° C. between the individual impregnation stages. After the last impregnation stage, the impregnated carrier is ^{dried at 120 °} C. for 16 hours and calcined at a temperature of 650 ° C. for 2 hours.

The catalyst produced in this way has the following composition:

66% by weight 4% by weight 20% by weight 10% by weight

Alumina Phosphorus pentoxide (PjOs) Molybdenum oxide (MoO,) Nickel oxide (NiO)

Catalyst B:

116 g of ammonium 2-phospho-5-molybdate are dissolved in 395 cm of water to which 100 cm ^{3 of} 27% ammonium hydroxide have been added.

117 g of sodium hexamine dichloride are dissolved in 800 cm ^{3 of} water to which 20 cm ^{3 of} 27% ammonium hydroxide have been added. The phosphomolybdate solution and the nickel hexamine dichloride solution are then mixed with one another.

25Og Alumlnlumoxld extrudates (see FIG. Preparation of Catalyst A) are then coated with the aqueous mixture containing the phosphomolybdate, the Nickelhexamlndlchlorld and the ammonium hydroxide, 10 ', impregnated minutes. This impregnation is repeated six times, the impregnated carrier being dried for 2 hours at 200 ° C. between the individual stages.

After the last impregnation, the carrier ίο dried for 2 hours at 120 ° C and then 2 Calcined at 650 ° C for hours.

The catalyst produced in this way has the following composition:

Aluminum oxide (AIjO ₁ ) phosphorpenoxide (PjO,) molybdenum _{oxide (MoO 1} ) nickel oxide (NlO)

66 wt. - ^{1 vol}

4 wt .- '\,

20 Ciew .- '\,

IO weight s,

150 g of catalyst B are used at 20 ° C. for 1 hour a mixture of 11 cm 4OiJgCm hydrogen fluoride and 90cm 'water impregnated. The fluorinated catalyst is then dried at 120 ° C. for 12 hours and Calcined at 650 ° C for 2 hours.

Catalyst C has the following composition:

Aluminum oxide (AljOi) phosphorus ^; ? ". ntoxkl (PjOi) molybdenum _{oxide (MoO 1} ) nickel oxide (NlO) fluorine (F)

64.0% by weight 3.9% by weight

19.4% by weight, 9.7% by weight 3.0% by weight

2) Hydrocracking trials.

A residual oil fraction obtained from a North African crude oil and deasphalted with liquid propane is used to improve the activity, selectivity and stability of the catalysts A, B and C to check.

This oil fraction has the following properties:

specific gravity 20/4 9.907

Viscosity at 99 ^a C 32.8 cSt Viscosity index (Vl,) ./. ASTM - D 2270 according to the Dewaxing at -19 ° C 77 Yield of dewaxed Oil after dewaxing

at -19 ° C 89.2% by weight

Certain amounts of this fraction of oil are over three identical beds from catalysts A, B and 'Ί passed under the following reaction conditions:

pressure

Space flow

speed

Hydrogen / oil relationship

140 bar

1 kg oil / h /] catalyst

1000 liters of H ₂ per kg of oil.

During the catalytic conversions, the temperatures are adjusted so that the products of the three treatments have a viscosity index (VI _£ ) of 130 after the components boiling below 375 ° C. have been removed by distillation and after dewaxing.

Dewaxing is done with the help of a mixture from methyl ethyl ketone and toluene (50:50) in a ratio of 3 parts by volume of mixture to 1 part by volume of oil carried out at a temperature of -19 ° C.

The following temperatures are in order to achieve the above Results required:

for catalyst A:
for catalyst B:
for catalyst C:

457 ° C 452 ° C 441 "C

for catalyst A:
for catalyst B:
for catalyst C:

Comparative experiment

A phosphorus-free catalyst is produced as follows:

A solution of 93 g of ammonium molybdate in 120 ml of water is _{mixed with a solution of 94 g of nickel formate in 108 ml of NH 4} OH (27% NH ₁ ).

250 g of Al ₂ Oi particles with a diameter of 1.3 mm obtained by extrusion are impregnated with this mixture for 10 minutes.

The impregnated particles are at for 2 hours 200 ° C and then subjected to the impregnation treatment again. Subsequently to the second drying treatment under the above conditions, the particles are 2 hours calcined at 650 ° C for a long time.

The finished catalyst consists of

70 wt% Al ₂ Oj
20 wt% MoO ₃
10% by weight NlO

It is tested under the conditions of Example 1. In order to obtain a lubricating oil (after removal of below 375 ° C boiling components and after dewaxing) with a Vl of 130, a hydrogenation temperature should be applied of 460 ⁰ C, which therefore substantially higher than for the inventive phosphorus-containing catalysts A and B of Example 1 with identical content of MoO ₃ and NiO.

In addition, the yield of dewaxed lubricating oil with an initial boiling point of 375 "C is only 23% by weight, compared with the yields according to the invention of 25 or 29% by weight when using catalysts A and B.

Exemplary embodiment 2

A residue fraction from a North African Crude oil was obtained, is deasphalted with the aid of liquid propane. The deasphalting residue has the following characteristics:

At these temperatures the following yield ?, of dewaxed oil with a VI of 130 and an initial boiling point of 375 ° C, based on the original North African used as the starting material Residual oil fraction, obtained:

25% by weight, 29% by weight \ 32% by weight

From the foregoing it can be seen that phosphorus halllge Catalysts have very good activity and selectivity for the production of lubricating oil with a show very high viscosity index and that these properties by preparing the catalysts with the help - ° Ammonium-2-phospho-5-molybdate and the addition of fluorine can be improved even more.

The three catalysts A, B and C also have one excellent stability. This can be seen from the fact that during the first 700 hours the temperature increased by about H. 2 ° C per 100 hours are increased muli in order to maintain the desired viscosity index VIj. = 130 guarantee while after 700 hours and up to end the experiments described above, that is, after 100 hours, the temperature was kept constant to achieve the desired result (VI, = 130) at any time.

35

40

45

50

55

65 specific weight 20/4

Viscosity at 37 ° C:

Viscosity index

(VI ,, ASTM 2270)

after dewaxing

at -19 ° c

Oil yield after

Dewaxing

at -19 ° C

0.907
32.8 cSt

77

89.2 wt .- '\,

This asphalt-free residual oil fraction becomes one catalytic hydrocracking treatment in the following Subject to conditions:

temperature

pressure

Space flow

speed

Hydrogen / ϋΐ-

Ratio

440 ° C
140 bar

1 kg oil / h / l catalyst
1000 liters / kg oil.

The hydrocracking catalyst has the following composition:

30 AhO,

PjO,

MoO,

NOK

SIO ₂

63.0% by weight 3.9% by weight

19.4% by weight 9.7% by weight 3.0% by weight 1.0 wt%

The fraction boiling below 400 ° C. represents 56% by weight of the hydrocracked product Hydrocracked product separated off by fractional distillation.

The fraction boiling above 400 ° C. (44% by weight) is mixed with 50 parts by volume Methyl ethyl ketone and 50 parts by volume of toluene in one Dewaxed temperature of -27 ° C. The solvent / oil ratio is 3: 1.

During the treatment, 12% by weight of soft paraffin precipitate.

The lubricating oil thus obtained has a viscosity index VI _£ (ASTM - D 2270) of 130.

The yield of this lubricating oil is 32% by weight based on the original asphalt-free residual oil fraction.

The soft paraffin obtained in dewaxing is then made using the following conditions catalytically hydroisomerized:

60

temperature 340 ° C pressure 140 bar Room flow speed 0.81 kg Soft paraffin / h / l catalyst Hydrogen/ Soft paraffin ratio 1.660 liters Hydrogen / kg Soft paraffin.

The hydroisomerization catalyst contains 17 Wt .-% tungsten, 9 wt .-% nickel and 2.5 wt .-% Fluorine, which is supported on a carrier of 26 wt .-% aluminum

xid. Remainder silicon oxide, are deposited. This catalyst was sulphurized by adding sulphurous gas oil 36 Hours has been passed under the following conditions:

temperature 350 "C pressure 50 bar Space flow speed: I kg oil / h / l catalyst Hydrogen/ Oil ratio ISO liter / kg oil

Fractional distillation removes the fraction boiling below 400 ° C. from the hydroisomerization product severed. The yield of residue boiling above 400 ° C. is 49.4% by weight, based on the Mydrolsomerization feed. This residue is at -27 ° C with the aid of a mixture of methyl ethyl ketone and toluene (50/50) depurated. where the Solvent / oil ratio is 8: 1.

The bulge of dewaxed lubricating oil is 24.9 üew.-Λ ,. based on the dihydroisomerization feed.

This lubricating oil has the following properties:

Velocity index 158 (Vl,., ASTM - D 2270) 30.60 cSt Kinematic viscosity at 38 ° C Kinematic viscosity 5.97 cSt at 99 'C

Comparison attempt:

A deasphalted residue fraction of the same Origin and composition as in example 2

■; The material used is kept at -27 ° C with the help of a Mixture of methyl ethyl ketone and toluene (50/50) deparaffinized, the solvent / oil ratio being 3: 1 cheats. 14% by weight of soft paraffin are separated off.

This soft paraffin is produced under the same conditions and with the aid of the same sulfurized catalyst hydrolsomerislert as in Example 2.

The fraction of the liquid Hydroisomeilslerungsprodukles boiling above 400 ° C is in the same

i) As in Example 2, dewaxed.

However, the yield of lubricating oil is only 20% by weight, based on the hydroisomerization restriction. The lubricating oil thus obtained has the following properties:

Viscosity index 100 cSt (VI ,, ASTM - D 2270) Kinematic viscose 195.3 cSt lüt at 38 ° C Kinematic viscosi 16.89 at 99 ° C

This lubricating oil is therefore of a lower quality than the product of Example 2.

Claims (2)

Patent claims: 1. A process for the production of a lubricating oil with a high viscosity index by hydrocracking a high-boiling mineral oil fraction at elevated pressure and elevated temperature in the presence of a catalyst composed of 3 to 16% by weight of nickel, 6 to 24% by weight of molybdenum or tungsten, each in a metallic, oxidic or sulphidic form and optionally 1 to 6% by weight of fluorine on a refractory oxide support, characterized in that the catalyst used also contains 1 to 12% by weight of phosphorus, calculated as PaO ₅ , that is below a temperature of 350 Up to 400 ° C boiling is portions of the hydrocracked product is distilled off and the lubricating oil residue is dewaxed, and that optionally the soft paraffin obtained during dewaxing is catalytically isomerized in the presence of a hydrogen-containing gas and the hydrolisomerizate is dewaxed to produce a lubricating oil with a very high viscosity index. 2. The method according to claim 1, characterized in that the hydrocracking and hydrolsomerization treatment carried out in the presence of the same catalyst.