JPS5918438B2 - Hydrocarbon conversion method - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to the catalytic hydrocracking of heavy hydrocarbon mixtures selected from the group consisting of slack wax and synthetic lubricating oil fractions.
The present invention relates to a method for producing a lubricating oil with a viscosity index of 11Q-160.

The yield of lubricating oil with a given viscosity index obtained by catalytic hydrocracking of a heavy hydrocarbon mixture depends on the hydrocracking reaction activity of the catalyst (referred to as "cracking activity") and the nitrogen content of the heavy hydrocarbon mixture. and varies significantly with aromatics content.

By carefully adjusting the cracking activity of the catalyst to the nitrogen and aromatics content of the feedstock, an optimal catalyst can be selected that provides the maximum achievable yield of the lubricating oil when used in the hydrocracking of said feedstock or feedstock. can be manufactured.

However, when this optimal catalyst is used for the hydrocracking of said feed oil to produce a lubricating oil having a viscosity index greater than or equal to the desired level of viscosity index, the maximum achievement of this lubricating oil obtained from said feed oil is Compared to the yield, lubricating oils with a high viscosity index can be obtained in surprisingly small yields.

This optimized catalyst can be used to reduce nitrogen and/or
The same applies to the case where a lubricating oil having the above-mentioned predetermined viscosity index is produced using a heavy hydrocarbon mixture having an aromatic content as a raw material.

In this case too, lubricating oils with a given viscosity index can be obtained in rather unsatisfactory yields compared to the maximum achievable yields of lubricating oils obtained from the feed oils in question.

In view of the above, conventional methods have been to produce lubricating oils with different viscosity indexes by hydrogenolyzing the same feed oil, or by hydrogenolyzing feed oils with different nitrogen and/or aromatics contents with the same viscosity index. In order to produce lubricating oils with different levels of decomposition activity, catalysts with different decomposition activities had to be used in each case.

The present inventor has discovered that the above-mentioned defects in lubricating oil production by hydrogenolysis can be avoided by adding a nitrogen compound to the hydrogenolysis reaction activity and conducting the hydrogenolysis reaction at a temperature of 375-450°C. .

The present invention therefore provides a method for producing lubricating oil by hydrogenolysis of a heavy hydrocarbon mixture selected from the group consisting of slack wax and synthetic lubricating oil fractions, wherein the heavy hydrocarbon mixture is doped with nitrogen compounds. There are
The present invention relates to a method for producing a lubricating oil having a viscosity index of 110 to 160, characterized by a hydrogenolysis temperature of 375°C to 450°C.

According to the present invention, the most suitable catalyst for producing a lubricating oil with a predetermined viscosity index by hydrogenolysis of a heavy hydrocarbon mixture can be used if a small amount of nitrogen compounds are added to the feed oil. It is then possible to produce a lubricating oil with a higher viscosity index in high yield from this feed oil.

According to the invention, if some amount of nitrogen compounds are added to the feedstock with low nitrogen and/or aromatics content, the optimal catalyst described above (i.e. hydrogenation of heavy hydrocarbon mixtures containing some nitrogen and aromatics) (Catalyst suitable for producing lubricating oil with a given viscosity index by decomposition)
It is possible to produce a lubricating oil having a predetermined viscosity index in high yield from the above-mentioned feed oil using the above-mentioned feed oil.

In general, the addition of nitrogen compounds to a feedstock in accordance with the present invention allows the use of a single catalyst to produce lubricating oils with different viscosity indices from the same feedstock, as well as lubricants with the same viscosity index from feedstocks with different nitrogen and aromatics contents. This means that lubricating oil can be produced in high yield.

The amount of nitrogen compounds to be added to the feed oil depends on the desired degree of viscosity index of the lubricating oil to be produced and on the nitrogen and aromatics content of the heavy hydrocarbon mixture used as the feed oil.

The amount of nitrogen added to the feed oil in the form of nitrogen compounds is, as a rule, less than 3000 ppH1 by weight and increases the higher the level of the desired viscosity index and the lower the nitrogen and aromatics content of the feed oil. .

The exact amount of added nitrogen in each case can be easily determined by carrying out a small number of preliminary experiments in which varying amounts of the nitrogen compound are added to the feed oil in question.

The nitrogen compounds that can be added to the feed oil in the process of the invention are preferably ammonia and nitrogen compounds that yield ammonia under the conditions of the process.

Suitable nitrogen compounds are, for example, ammonia, ammonium hydroxide, alkylamines such as mono-, di-, trimethylamine and mono-, di-, triethylamine, alkanolamines such as mono-, di-, triethanolamine, These include arylamines such as mono-, di-, and triphenylamine, mixed alkylarylamines such as phenylethylamine, alkyldiamines such as ethylenediamine, and aryldiamines such as phenylenediamine.

Although relatively low molecular weight amines have been described, higher molecular weight compounds belonging to various homologous series can be used as well.

These nitrogen-containing compounds are, for example, organic nitrates, nitrites, nitriles, nitroso compounds, amides, imides, ammonia salts (for example ammonium acetate).
, urea and its derivatives, cyanate esters, isocyanate esters, incyanides, quaternary ammonium compounds, nitro compounds, pyridine and its derivatives such as quinoline and piperidine, oximes, hydroxylamines and azo compounds.

At least a portion of the amount of nitrogen added to the feed oil may be derived from ammonia isolated from the hydrocracking product and recycled to the hydrocracking reactor.

The production of lubricating oils of the present invention involves the use of Group VIB, Group IVB and Preference is given to using catalysts containing one or more metals of Group 1.

Suitable metals are, for example, nickel, cobalt, molybdenum and tungsten.

A catalyst comprising at least one metal selected from the group consisting of nickel and cobalt and at least one metal selected from the group consisting of molybdenum and tungsten, in particular 0.025-0.0.0 g of nickel and/or cobalt per 100 g of support. 8 especially 0.05-0.7 gram atoms and 0.05 molybdenum and/or tungsten
Catalysts containing -0.5 and especially 0.1-0.4 gram atoms are preferred.

Further, the atomic ratio of nickel and/or cobalt on the one hand and molybdenum and/or tungsten on the other hand is preferably in the range of 0.1:1 to 2:1, especially 0.2:1 to 1.
．． It is within the range of 6:1.

The metal may be prepared by any method known in the art for producing supported catalysts, such as by co-impregnating the support with a hydroxyl solution containing the metal salt in one or more steps, which is then dried and calcined. Leverage metals can be included in the catalyst.

The metal may be present on the support as a metal or as a metal oxide or as a metal sulfide.

Preferably, the catalyst is used in its sulfide form.

The catalyst may be sulphidized by any of the techniques known in the art to sulphide the catalyst, such as by combining the catalyst with a mixture of hydrogen and hydrogen sulfide, or with hydrogen and a sulfur-containing hydrocarbon oil, such as a sulfur-containing hydrocarbon oil. This can be done by contacting with gas oil.

Catalyst supports suitable for use according to the invention are, for example, silica, alumina, zirconia and magnesia and mixtures of these oxides, such as silica-alumina, silica-magnesia and silica-zirconia.

Catalysts containing alumina or silica-zirconia as support material are preferred.

The catalyst used according to the invention may further contain promoters such as fluorine, boron and phosphorus.

Fluorine may be added to the catalyst at any stage of catalyst manufacture.

Fluorine may also be added to the catalyst at an early stage of hydrocracking (eg, during or just after start-up of the unit) by directly fluorinating the catalyst.

In situ fluorination of the catalyst can be carried out by adding a suitable fluorine compound to the gaseous and/or liquid feed stream that is passed over the catalyst.

The amount of fluorine present in the catalyst used according to the invention is preferably from 0.5 to 7% by weight.

For producing lubricating oils according to the invention, it is preferred to use one of the following types of catalysts:

That is, a porous carrier is impregnated with a solution containing (a) one or more compounds of metals selected from the group consisting of nickel, cobalt, molybdenum and tungsten, and (b) phosphate ions Q→ peroxide ions; The composite is then dried and calcined to produce a catalyst.

A fluorine-containing supported catalyst containing at least one metal selected from the group consisting of nickel, cobalt, molybdenum and tungsten, in which at least a portion of the fluorine is added to the catalyst by being fluorinated as is.

One or more metal compounds selected from the group consisting of nickel, cobalt, molybdenum and tungsten are added in a sufficient amount such that the finished catalyst contains 30 to 65% by weight of these metals expressed as metal oxides. When dried and sintered from an aqueous solution with a concentration of 0.75 to 1.6
Packed bulk density of 9/vtl and 0.15-0.51 rL
A catalyst prepared by adding to an alumina hydrogel giving a pserogel with a pore volume of l/g followed by drying and calcination of this composite.

A composition containing one or more metal sulfides selected from the group consisting of nickel, cobalt, molybdenum and tungsten, a porous carrier, a water-soluble salt of one or more of the above metals, and water. A supported catalyst prepared by treating a material with a hydrogen sulfide-containing gas at a humidity below 150°C and then heating this material in a hydrogen-containing gas to a final temperature above 200°C. The amount of water present in the composition to be treated with is the amount of water present in the composition after drying the composition at 100° C. in a drying gas, such that the dried composition is inside the pores of the carrier. The catalyst corresponds to an amount of water that is increased by 20 to 120% of the amount of water that can be absorbed at 20°C.

Heavy hydrocarbon mixtures that can be used as starting materials for the production of lubricating oils according to the present invention include synthetic lubricating oil fractions obtained during vacuum distillation of atmospheric distillation residues of synthetic crude oils, and these synthetic lubricating oil fractions. Waxes separated from synthetic lubricating oil fractions obtained by fractionation or hydrogenolysis, ie, slack wax, are preferred.

The above synthetic lubricating oil fraction is, for example, spindle oil (SO
), light machinery oil (LMO) and medium heavy machinery oil (MM
The synthetic fiber distillate of O), the synthetic fiber extraction residue of de-asphalted oil, spindle oil, light machinery oil and intermediate heavy machinery oil, and the above-mentioned lubricating oil fraction are treated with a solvent selective for aromatics such as furfural to produce the above-mentioned lubrication. Synthetic fiber brightstock obtained from oil fractions, and spindle oil, light machine oil, intermediate heavy machinery oil, deasphalted oil, and brightstock slack wax obtained by dewaxing from the above-mentioned lubricating oil fractions.

Regarding the viscosity index of the above-mentioned spindle oil, light machinery oil, and intermediate heavy machinery oil, the viscosity index of this type of oil is generally 9.
The value is within the range of 5-105.

Slack wax is known to have a high viscosity index per se, ie, its viscosity index may be higher than that of lubricating oil products.

Slack wax is about 160, for example 155
It can be used as a raw material for producing lubricating oil products with a high viscosity index of -158.

one or more distillate lubricating oil fractions and/or one or more residual lubricating oil fractions and/or one or more distillate lubricating oil fractions and/or one or more residual lubricating oil fractions;
Species or mixtures of two or more slack waxes can also be used as starting materials for the production of lubricating oils according to the invention.

Very interesting results can be obtained using the following hydrocarbon mixtures as starting materials.

That is, deasphalted residual petroleum fractions and oil residues produced by treating these deasphalted petroleum fractions or cycle oils of heavy catalytic cracking units with solvents that are selective for aromatics such as furfural. It's oil.

The nitrogen content of these heavy hydrocarbon fractions before addition of nitrogen-containing compounds according to the invention is 3000 p11 by weight.
Preferably, the amount is less than 11.

Hydrocracking of heavy hydrocarbon fractions for the production of lubricating oils according to the present invention is carried out preferably by adding the required amount of nitrogen to the heavy hydrocarbon fraction and then treating it at elevated temperature and pressure in the presence of hydrogen. is carried out in contact with a suitable catalyst present in a bed or beds of particles ranging in size from 0.5 to 31/L7IL.

Suitable hydrogenolysis conditions are a temperature of 375-450°C and a pressure of 5-450°C.
250 bar, the hydrogen to feed ratio is 100 to 500 ONl hydrogen per liter of feed oil, and a space velocity catalyst of 11
It is 0.2 to 5.0 boils per hour per feeding oil.

The following conditions: temperature 375-425℃, pressure 100℃
~200 bar, the ratio of hydrogen to feed oil is 500-250 ON# of hydrogen per 1 ky of feed oil, and the space velocity is 1 kg of catalyst.
It is more preferred to use 0.5 to 1.5 kg per hour.

Lubricating oils produced by the method of the present invention have a low aromatics content.

A lubricating oil with an even lower aromatics content can be obtained by performing a hydrofinishing step after the hydrogenolysis step.
It can be produced by the method of the present invention.

Hydrofinishing of the hydrogenated cracked oil can be accomplished by contacting the hydrogenated cracked oil with a hydrofinishing catalyst at elevated temperature and pressure, and in the presence of hydrogen.

the pressure used in the hydrofinishing process;
The space velocity and gas proportions can be chosen within the same ranges as above for the hydrocracking step.

The temperature of hydrofinishing is preferably 225-4
It is selected within the range of 00°C, particularly within the range of 275 to 375°C.

Just the right temperature for the hydrofinishing process is at least 25°C below the humidity at which the hydrolysis takes place.
Must be at a low temperature.

A suitable hydrofinishing catalyst is
It is a catalyst containing one or more metals of Group 1, Group 1B, and/or Group 2.

The effluent of the hydrocracking reactor, or if hydrofinishing is applied, the effluent from the hydrofinishing reactor, is cooled and separated into a hydrogen-rich gas and a liquid product.

The liquid product includes hydrocarbons boiling below the boiling range of the lubricating oil and hydrocarbons boiling within said range.

Hydrocarbons boiling below this range are preferably separated from the high-boiling residue by fractional distillation.

The cutting point of this distillation is
Preferably, the high boiling resid is selected to have an initial boiling point of 350-550°C.

In addition to being an excellent lubricant component, this residual oil usually solidifies at ambient temperatures, thus having an adverse effect on the pour point of the lubricant.
- Contains paraffin.

Therefore, in order to produce a suitable lubricating oil from the residual oil, it is preferable to dewax the residual oil.

The dewaxing treatment can be carried out by any desired method.

Dewaxing is done using methyl ethyl ketone and toluene -10
Preferably, it is carried out at a temperature in the range of -40 DEG C. and with a solvent to oil volume ratio in the range of 1=1 to 10:1.

To increase the lubricating oil yield, it is preferred to recycle at least a portion of the separated wax to the hydrocracking process.

The following test examples are shown to explain the present invention in more detail.

Eight types of catalysts [(i) to (e)] were used in the hydrogenolysis for producing lubricating oil from nine types of heavy hydrocarbon mixtures (i-■).
It was used.

The composition of the catalyst and the charged oil were as follows.

Catalyst (a): Ni/Mo/P/Al containing nickel 0.06.9 atoms, molybdenum 0.159 atoms and phosphorus weight ratio 3.19 per 100 g of alumina weight ratio
203 catalyst.

The catalyst was prepared by impregnating alumina with an aqueous solution containing nickel nitrate, phosphoric acid, ammonium molybdate, and hydrogen peroxide, then drying and calcining the composite.

Catalyst (0): Ni/Mo/P containing 2.6% by weight of fluorine
/F/Al□03 catalyst.

This catalyst was produced by impregnating the catalyst (a) with an aqueous solution of ammonium fluoride, then drying and calcining this composite.

Catalyst (/→: Ni/Mo/P containing 4.6% by weight of fluorine
/F/Al□03 catalyst.

The catalyst was prepared by fluorination without isolation of the catalyst.

catalyst): nickel 31% per 100 parts by weight of alumina.
Ni containing 0 parts by weight and 58.0 parts by weight of tungsten
/W/F/Al□03 catalyst.

The catalyst was prepared by mixing alumina hydrogel with an aqueous solution containing nickel nitrate, ammonium tungstate, and ammonium fluoride, the pH of which was adjusted to 6.5 with 25% ammonium.

The mixture was heated to 80° C., filtered to remove the gel, extruded, dried and fired.

The alumina used in the preparation of this catalyst, when dried and calcined, has a compact bulk density in the range of 0.75-1.6 g/rfLl and a pore volume of 0.15-0.5 ml/g (D It became xerotic.

Catalyst (E): 3.0% nickel per 100 parts by weight of alumina.
3 parts by weight, 25.4 parts by weight of tungsten and 3.7% by weight of fluorine.

This catalyst was manufactured by impregnating alumina with an aqueous solution of ammonium tungstate and nickel nitrate.

After adjusting the humidity to 100%, apply this composition to
treated with H2S for 16 h at 5 bar (gauge) and 75 °C, then in a H2 stream containing H2S (9% by volume of H2S).
, IQ bar/l/(gauge), 25,000 Nil/
IJ/h) within 2 hours to 400°C and finally held at 400°C for about 2 hours in this air flow (hereinafter the term "humidity" is used) It means the water contained in the composition in addition to the water contained in the composition after drying.

Wetness is expressed as the percentage of water that the dry composition retains within the pores of the carrier at 20'C).

Fluorine was introduced into the catalyst by neat fluorination.

Catalysts (H) and (H): Ni/W/ containing 6.6 parts by weight of nickel and 50.8 parts by weight of tungsten per 10 parts by weight of alumina, and 1.1% and 3.1% by weight of fluorine, respectively. F/Al□03 catalyst.

These catalysts were manufactured in the same manner as catalyst (e).

Catalyst (J-): 1 nickel per 100 parts by weight of alumina
1.9 parts by weight, 20.1 parts by weight of molybdenum and 2 parts by weight of phosphorus.
．． Ni/Mo/ containing 6 parts by weight and 2% by weight of fluorine
P/F/Al2O3 catalyst.

Fluorine was introduced into the catalyst by neat fluorination.

To fluorinate catalysts (c), (e), (f), (t), and (a) as they are, ortho-fluorotoluene is added to the feed oil in the early stage of hydrogenolysis. It was done.

For preparation oil Residue from de-asphalt distillation of Middle Eastern crude oil.

Nitrogen content near 60% by weight, aromatics content = 5
7% by weight, viscosity index after dewaxing at -30°C = 78°. Charge oil ■: Oil in which 45 Qppm of nitrogen as pyridine was added to charge oil I.

Prepared oil ■: An oil obtained by adding 900 Wm of nitrogen as pyridine to the prepared oil I.

Preparation oil: Extracted residual oil remaining after extracting stock oil I with furfural.

Nitrogen content: 320 ppm by weight, aromatics content = 47% by weight, viscosity index after dewaxing at -30°C: 93° Stock oil ■: Oil in which 450 parts by weight of nitrogen as pyridine was added to stock oil ■.

Prepared oil ■: An oil obtained by adding 900 ppm by weight of nitrogen as pyridine to the prepared oil ■.

Charged oil ■: Extracted residual oil remaining after heavy catalytic cracking circulating oil is extracted with furfural.

Basic nitrogen content: 2 weight solution, aromatics content:
27.3 mmol / 100 g, 20% by volume of UPO distillation method Distillation point: 420'C Viscosity index after dewaxing at 1-27°C: 117° Charge oil ■: Nitrogen as tri-n-butylamine in charge oil ■ Oil added with 100 ppm by weight.

Feeding oil ■: Feeding oil ■ An oil to which 200 parts by weight of nitrogen was added as n-butylamine.

The viscosity index shown in the test examples herein is ASTM
It was measured based on method D2270.

Hydrogenolysis tests 1 to 6 were conducted under the following conditions.

Pressure 150 barLiquid space velocity (
LH8V) 11/llb gas ratio
200ONl/kg catalyst bed 100g Catalyst size Q, 5-1.4mm The catalyst was used in the form of sulfide.

The sulfurization of catalysts (a) to ii) and iii) was carried out by contacting the catalysts with hydrogen and sulfur-containing gas oil.

Dewaxing was carried out using a 1:1 mixture of methyl ethyl ketone and toluene.0 Test I Hydrogenolysis of feed oils I, IV, V and (2) over a catalyst (b) and topping at 400°C.

After dewaxing at -30°C, the viscosity index is 130 and 1, respectively.
A lubricating oil having a pH of 40 was produced.

Required temperature (temperature that should be applied to obtain the lubricating oil)
and the yield of dewaxed oil are shown in Table 1.

The numerical values shown in Table 1 indicate the following items.

The viscosity index of the stock oil ■ is higher than that of the stock oil 1 (93 vs. 78
), with catalyst (0), although the temperature required to produce lubricating oils with viscosity indexes of 130 and 140 from feed oil ■ is lower than when producing from feed oil I, these lubricating oils can be produced from feed oil ■. The yield obtained is lower than that obtained from feed oil I.

This means that the catalyst (using a viscosity index of 130 and 1
This indicates that feed oil N is more unsuitable than feed oil I for the production of lubricating oil No. 40.

By adding nitrogen compounds to the stocking oil (stocking oil)
The yield of lubricating oils with viscosity indexes of 130 and 140 from the above feed oils using catalyst (D) is significantly increased. .

Test 2 By hydrogenolyzing the feed oil ■ on the catalyst (a),
Lubricant oils were produced having viscosity indexes of 130 and 140 after topping at 00°C and dewaxing at -30°C, respectively.

The required temperature and dewaxed oil treatment are shown in Table 2.

For comparison, the results of Test 1, in which feed oil ■ was hydrogenolyzed over a catalyst, are also shown in the table.

The values shown in Table (1) indicate that catalyst (A), like catalyst (B), is not very suitable for producing lubricating oils with viscosity indexes of 130 and 140 from feed oil (2).

(Compared to catalyst (a), catalyst (a) shows a higher yield of the lubricating oil but a much higher temperature requirement.

) Test 3 By hydrogenolyzing feed oils I and ■ over catalysts (p) and (c), a lubricating oil having a viscosity index of 110 after topping at 400°C and dewaxing at -30°C was produced. .

The required temperature and the yield of dewaxed oil are shown in Table 2.

The values shown in Table ■ indicate that catalyst (C) is even more unsuitable for producing lubricating oil with a viscosity index of 110 from pre-charge I.If a nitrogen compound is added to pre-charge I (feed oil = 450 weight ppm of nitrogen in the feed oil I), the catalyst (c) shows the same excellent performance as the catalyst (0).

Test 4 Topping was performed at 400°C by hydrogenolyzing pre-preparation I and ■ on catalysts (H) and (H), and -
A lubricating oil was produced having a viscosity index of 130 after dewaxing at 30°C.

The required temperature and the yield of dewaxed oil are shown in Table 2.

The values shown in Table (1) indicate that catalyst (G) is even more unsuitable than catalyst (F) for producing lubricating oil with a viscosity index of 130 from (1) before preparation.

When a nitrogen compound is added to pre-preparation I (preparation oil ■ - preparation oil I 10 nitrogen 900 ppm by weight), the catalyst (g) becomes the catalyst (g)
shows comparable performance.

Catalysts (H) and (T) are both made from the same Ni/W/Al 203 catalyst by fluorination in situ and differ only in fluorine content (catalyst (
) contains 1.1% by weight of fluorine, and the catalyst (g) contains 3.1% fluorine.
weight%).

The test results of the present invention demonstrate another interesting feature of the present invention.

If excess fluorine is added due to some kind of operational error during the fluorination of the catalyst as is, there is no need to replace it with a catalyst with lower fluorine content, but rather the amount of nitrogen compounds is sufficient.

Test 5 Topping was performed at 400°C by hydrogenolyzing pre-preparation I and
Lubricating oils were produced having viscosity indices after dewaxing at 130 and 140, respectively.

The required temperature and yield of dewaxed oil are as shown in Section V.

The numerical values shown before the catalyst (e) are more suitable for the production of lubricating oil with a viscosity index of 130 from the pre-charge I than the catalyst (e), but the catalyst (e) has a viscosity index of 130 from index 1
This shows that it is more unsuitable than the catalyst (b) for producing lubricating oil of No. 40.

When a nitrogen compound is added to ■ before preparation (preparation oil ■ - preparation oil I
〇Test to significantly increase the yield of lubricating oil with ten nitrogen 450 and severity index 140 6. Before preparation, by hydrogenolyzing the lubricating oil with A lubricating oil with a viscosity index of 140 was produced.

The required temperature and the yield of dewaxed oil are shown in Table 2.

The yield of lubricating oil with a viscosity index of 140 from feed oil ■ using (the numerical values shown in Table ■) for the catalyst is as follows: When nitrogen compounds are added to the feed oil (feed oil l = feed oil I 10 nitrogen 900 ppm by weight) ) shows a significant increase.

Test 7 A lubricating oil having a viscosity index of 139 after being topped at 400°C and dewaxed at -27°C was produced by hydrogenolyzing the feed oils (1), (2) and (2) over a catalyst (e).

This hydrogenolysis test was conducted under the following conditions.

Temperature 402℃ Pressure 140 bar Weight space velocity (WH8V) 0.8kg/A/h Gas ratio
175ON7/kg catalyst bed 25o
rILl Catalyst size: 1.5 The behavior of the dewaxed oil is as shown in Table 2.

The values shown in Table 1 indicate that the yield of lubricating oil with a viscosity index of 130 from feed oil ■ using catalyst (7) is as follows: When a nitrogen compound is added to the feed oil (feed oil ■ = feed oil ■ ten nitrogen 10
0 ppm by weight, preparation oil ■ = preparation oil ■ 10 nitrogen 200 ppm by weight
pm), indicating a significant increase.

Test 8 Using a catalyst bed containing 160 rILl of catalyst containing 15.0 parts by weight of nickel and 30 parts by weight of tungsten per 100 parts by weight of alumina and containing about 5% by weight of fluorine,
Bright stock slack wax from the Middle East containing 200 ppm (w) of N as pyridine was heated to -1 pressure.
50 bar, temperature -386°C, LSHV=11. /l(
Catalyst) At 7 o'clock, a lubricating oil with a viscosity index of 157 was produced by hydrogenolysis.

As illustrated in Tests 1-8, the effects of the present invention are as follows:
Lubricating oils with a viscosity index of 110 to 16Q can be produced in high yield by hydrocracking of various types of heavy hydrocarbon mixtures.

However, the leverage effect is not limited only when using feedstocks with a viscosity index lower than that of the lubricating oil product, but can also be obtained when using feedstocks with a higher viscosity index than the lubricating oil product. It will be done.

The experimental results described in Test 8 demonstrate this effect, ie, demonstrate that superior lubricating oils can be produced even from feedstocks with extremely high viscosity indexes.

Thus, the method of the present invention is a very flexible method, which is considered to be of great practical importance.

Claims (1)

[Claims] 1. A method for producing lubricating oil by hydrogenolysis of a heavy hydrocarbon mixture selected from the group consisting of slack wax and synthetic lubricating oil fractions, wherein the heavy hydrocarbon mixture is one to which a nitrogen compound is added. A method for producing a lubricating oil having a viscosity index of 110 to 160, characterized in that the hydrogenolysis temperature is from 375°C to 450°C.