DE2405116A1 - METHOD FOR PRODUCING LUBRICATING OILS - Google Patents

Description

PATENT LAWYERS

DR.-ING. BY KREISLER DR.-ING. SCHDNWALD DR.-ING. TH. MEYER DR. FUES DIPL.-CHEM. ALEK VON KREISLER DIPL-CHEM. CAROLA KELLER DR.-ING. KLDPSCH DIPL.-ING. SELTING

5 COLOGNE 1, DEICHMANNHAUS 2 A · O 5 1 1 6

Cologne, February 1st Ke / Ax

The British Petroleum Company Limited, Britannic House, Moor Lane, London EC2Y 9BU (England). Process for the production of lubricating oils

The invention relates to the manufacture of lubricating oils, particularly a wide range of lubricating oils.

The main steps in the production of lubricating oils from petroleum fractions are a) the removal of aromatics, whereby an improved viscosity index is obtained, and b) the dewaxing and dewaxing by which the pour point is improved. Solvents are usually used in both stages to achieve the desired To obtain results, however, hydrocatalytic treatments for both stages have also been suggested as alternatives. Each of the four methods has its advantages and disadvantages. According to the invention, the four processes become particular Combined in such a way that the best utilization of the possibilities inherent in each process is achieved and the application procedures are avoided for tasks for which they are not suitable.

The method according to the invention for making a range of lubricating oils is characterized in that petroleum fractions boiling above 350 ° C. are divided into at least one lighter fraction and at least one heavier fraction

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Fraction separates the lighter fraction or the lighter fractions partly or entirely in a hydrocatalytic one Dewaxing and dewaxing process and one Solvent extraction to remove aromatics and the heavier fraction "or the heavier fractions whole or partially a hydrocatalytic treatment to improve the viscosity index and a dewaxing and Subjected to dewaxing with solvents.

The term "lubricating oil" as used herein includes lubricating oils for every purpose as well as special oils that are used in the lubricating oil sector boil, e.g. transformer oils. A special feature of the invention is that it allows manufacturing a wide range of oils from light spindle oils to heavy automotive oils made from bright stocks.

The point of intersection between the lighter and heavier fractions or the lighter and heavier fractions is preferably in the range from 450 ° to 500 ° C.

The number of products formed from the lighter fraction is expediently 2 to 4. For example, spindle oils and the two lightest types of automotive lubricating oil can be used getting produced.

As already mentioned, the treatment of the lighter fraction or fractions is carried out by a combination of hydrocatalytic Dewaxing and dewaxing and solvent extraction to remove aromatics. The proceedings can be carried out in any order, but the hydrocatalytic dewaxing and Dewaxing is preferably done first. A single Fraction treated in a further boiling range in the sequence of processes and then distilled or a number of fractions can be treated in separate steps. Preferred is the the latter way.

In the preferred hydro-catalytic process for dewaxing and deparaffining passing the lighter fraction "or the lighter fractions, together with hydrogen" at a temperature of 250 ° "to 500 ⁰ C and a pressure of 7" to 200 bar (gauge pressure) over a catalyst , which contains one or more hydrogenation components from groups VIa and VIII of the periodic table, which are incorporated into a crystalline mordenite with a reduced alkali metal content. This treatment can be carried out by the general procedure described in British Patents 1,088,933 and 1,134,014.

A special feature and a special advantage of dewaxing and dewaxing by catalytic hydrogenation is the ability of the process, in the case of the lighter fractions used according to the invention, which normally have pour points of 20 ° to 45 ° C., to low pour points of -50 ° to -18 ⁰ C to outgrow. These low pour points can only be achieved at enormous expense by dewaxing and dewaxing with solvents. So far they have been achieved by dewaxing and dewaxing with urea, but this is a relatively expensive process.

The wax in these lighter fractions consists of crystalline wax or paraffin wax, e.g. n-paraffins or slightly branched paraffins, and becomes selectively low-boiling paraffins, especially CV and C. paraffins cracked. The selective breakdown of the paraffin wax hydrocarbons is based on the nature of the catalyst Mordenite based on the selective attack on these hydrocarbons, but not on the others Hydrocarbons present in the starting material are favored.

The catalytic dewaxing and dewaxing can

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at a temperature in the already mentioned range from 250 to 500 C and at a pressure in the already mentioned Range from 7 to 200 bar (manometer pressure) and at a room air velocity between 0.1 and 20.0 V / V / h and with a hydrogen consumption of 90 to 3600 m / m can be carried out. Preferably, catalytic dewaxing and dewaxing are among the performed under the following conditions:

Temperature 265-43O ° C

Room flow rate 0.5 - 10.0 V / V / hour.

Pressure (gauge pressure) 4-0 - 200 bar

Hydrogen consumption "900 - 2700 m ⁵ / m ⁵

The expression "crystalline mordenite with reduced alkali metal content" preferably means a mordenite with an alkali metal content of less than 3 wt .- ^. Of the Deficiency or deficiency of alkali metal cations can be caused by other metal cations, e.g. cations of metals of the II group, especially magnesium or rare earth metal cations, are balanced. Preferably the mordenite is however, a "decationized mordenite", i.e. a mordenite deficient in metal cations. Another in technical terminology The term used for such a mordenite is the expression "hydrogen mordenite", since it is assumed that metal cations that are removed are replaced by hydrogen ions. However, since the detection of hydrogen ions is not possible in zeolites, the exact structure remains uncertain. A cation deficit can, however on the other hand, can be easily measured by analyzing the metal elements present in the zeolite.

Natural or freshly made synthetic mordenite has the formula

1 Me ₂ 0: Al ₂ 0 ₃ : 9-11 SiO ₂ .XH ₂ O j

in which Me is a metal cation and η is the valence of the cation and X as a function of deη temperatures that the

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Mordenite went through during his treatment varied between 0 and 7. Me is usually sodium, and at A common form of decationization is sodium morden with a base exchange with ammonium cations subject. The ammonium form is then heated to drive off the ammonia, the hydrogen form or the decationized mordenite left behind. In the second method, the mordenite can be treated with a mineral acid, e.g. Hydrochloric acid or sulfuric acid, to decationize the mordenite directly. A combination of Acid treatment and ammonium treatment can also be used.

The decationized mordenite used for the purposes of the invention preferably has a silica / alumina ratio, that is higher than normal and at least 14: 1. In special cases ratios were up to 90: 1 is reached, so that a ratio of 100: 1 is to be regarded as a practical upper limit. Particularly preferred silica / alumina ratios are in the range from 14s1 to 50: 1.

It has been found that through certain decationization treatments Aluminum and the desired metal cations can be removed. The one for the purposes is therefore appropriate of the invention used mordenite, the silica / alumina ratio of which is higher than normal, by treatment a mordenite containing metal cations, in particular mordenite, with a strong acid, e.g.

Sulfuric acid or hydrochloric acid, with a concentration of 5 to 50 wt .-%, preferably 10 to 20 wt .- % _t . A single treatment or two or more consecutive treatments can be carried out with acids of the above concentrations. Appropriate is a method in which the mordenite is treated with the acid under reflux for 2 to 12 hours.

In the decationized mordenite, the content of the remaining Metal cations, for example sodium cations, less than 3 wt. 56, preferably less than 1.5 wt. 56 des Mordenits amount.

It should be emphasized that mordenites whose silica / alumina ratios are higher than normal, the Preserve the crystal structure of the mordenite and in terms of physical strength, stability or crystallinity are not significantly changed.

A platinum group metal, in particular platinum or palladium, is preferably used as the hydrogenation component. This metal is preferably introduced by ion exchange. The amount of the platinum group metal is preferably in the range from 0.01 to 10% by weight, in particular im Range from 0.1 to 5 wt. However, good results are also obtained with iron group metals, in particular nickel. These metals can be discarded in amounts similar to the platinum group metals. Mixtures, of course Metals and metal compounds from YI. and VIII group, e.g. cobalt and molybdenum can also be used. ";

The catalyst is ealciniert prior to use, preferably at a temperature, for example 25O ° to 600 ⁰ C, to any water and ligands, which are bound to the hydrogenation to remove.

The product from dewaxing and dewaxing can be distilled to below the boiling point of the starting material to remove simmering light ends. As already mentioned, these are mainly CU and C paraffins, which are valuable as raw materials in the petrochemical industry or as liquefied petroleum gas (LPG).

The product of dewaxing and dewaxing becomes then select with a to remove aromatics

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Solvent "treated. By dewaxing and dewaxing the viscosity index is lowered, and regardless of this, the dewaxing of the solvent extraction precedes or not, some viscosity index improvement is usually necessary to achieve this To reverse the lowering of the viscosity index at least partially and the viscosity index occasionally to one Increase value above its original level. In the case of the lighter fractions subjected to the treatment the required viscosity index values for the product are typically in the range of 0.1 "to 100 and through Solvent extraction of these starting materials can provide such viscosity index values efficiently and economically reach.

Sulfur dioxide / benzene, phenol, glycol and preferably furfural are suitable solvents. The solvent can be used in a column with fixed internals or in a column provided with a rotating disk with 1 to 20 theoretical extraction stages. The main process variables are the Lösungsmlttel / oil ratio 0.5: 1 may be, the average temperature 15 ° to 150 ^0: 1 to 5: 1 (volume), in particular 1.5: 1 to 4.0 C, in particular 30 ° to 130 ° C, and the temperature gradient in the column, which can be between the following limits: Temperature at the top of the column 150 ° C maximum

Temperature at the column foot '38 ° to 121 ⁰ C.

The separation of the extract and the raffinate and the isolation and recycling of the solvent can take place according to usual methods.

The heavier fraction or fractions boiling above the cut point may be able to remove the residue together with one or more heavier distillates. This part of the original

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As already mentioned, the feedstock is obtained through the combination of hydrocatalytic viscosity index improvement and solvent dewaxing and dewaxing "Treated. These treatments can be carried out in any order, but with the viscosity index improvement first is made * The starting material can be closed with subsequent distillative Separation treated in product fractions or preferably first separated into fractions that are separated for be guided through the stages of treatment. Preferably the feed is separated into at least two fractions, namely a vacuum distillate and one Vacuum recovery, of which parts may be subsequently can be mixed again.

The vacuum residue contains asphaltenes and possibly organometallic compounds and can therefore be entasphaled before the hydrocatalytic treatment. Suitable solvents for deasphalting to low-η-paraffins, in particular propane, are the 20 to 100 ⁰ C, preferably at 40 ° to 80 ⁰ C, a pressure of 5 to 50 bar, preferably 25 to 35 bar (gauge pressure) and solvent / Oil volume ratios of 1: 1 to 20: 1, preferably 5: 1 to 13: 1, can be used.

For the hydrocatalytic viscosity index improvement, a treatment is preferred in which the heavier one Fraction or heavier fractions over a catalyst, which one or more hydrogenation components from the Contains groups VIa and VIII of the periodic table on a refractory oxide carrier, together with hydrogen at a temperature of 340 ° to 460 ° C and a pressure from 70 to 210 bar (manometer pressure).

The hydrocatalytic viscosity index enhancement can be applied to produce products with a moderate viscosity index, e.g. 75 to 100, or a high viscosity index

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from "e.g. 101 to 150 to form". A special The advantage of this treatment is this flexibility. High viscosity index oils are not just for certain special Purposes, but also "particularly advantageous in that they eliminate the need to use viscosity index improvers in high-grade oils reduce or switch off and such oils with high viscosity index not easily or produced economically by solvent extraction can be. The viscosity index is hereinafter referred to by the abbreviation "VI".

As part of the hydrocatalytic treatment to improve VI two general procedures are possible. These are 1) a relatively mild treatment with a moderate one VI improvement for example to 75 to 100 after dewaxing and dewaxing with minimal degradation and minimal decrease in viscosity. An increase in the VI of the product to such an extent that the oil, if desired, denies Multigrade oil requirements can be achieved using known polymeric VI improvers will. 2) A more severe treatment with extensive degradation and extensive viscosity reduction, but with greater VI improvement to, for example, more than 100 VI after dewaxing. A larger amount of lower boiling gas oil, kerosene and gasoline than By-products are obtained in the harsher treatment.

The working conditions for the two working methods can be from the following general and preferred ranges to get voted:

Veiter Mild Sharper Area Treatment Treatment

QJ (2)

Temperature, ⁰ C 340-460 340-430 380-460 Gauge pressure, bar 70-210 70-170 120-210

Room air velocity, V / V / hr. 0.1-5 0.5-2 0.2-2 hydrogen consumption, m ⁵ / m ⁵ 360-1800 360-1800 "360-1800

One or more refractory inorganic oxides of elements of II., III. or IV. Group of the periodic table. These oxides can contain halogen. Preferably the amounts are of the components of the carrier selected from the following areas:

Al ₂ O ₃ 10 Ms 100 wt. 56

SiO ₂ 0 to 90 »

B ₂ O ₃ 0 to 25 "

P or Cl O "to 15

One or more oxides or sulfides of metals from group VIa (chromium, Molybdenum or tungsten) and metals of the iron group (iron, cobalt or nickel) are used. When platinum group metals are used, they are expediently in metal form. The amounts of the hydrogenation components can be in the following Areas are:

Group VIa metals 2-25 wt .- $ (expressed as

Metal)

Iron group metals 1-15% by weight ⁿ platelet metals 0.1-5 ^{% by weight w}

Preferred hydrogenation components are 2 to 25% by weight Molybdenum (expressed as metal, but present as oxide or sulfide) and 1 to 15 wt .- ^ nickel and / or cobalt (also expressed as metal, but present as, oxide or sulphide).

For the procedure (1), the preferred support contains 50 to 90 wt .- ^ Al ₂ O ₅ and 10 to 50 wt .- # SiO ₂ . In the procedure (2), the same carrier is preferably used. The increased severity of the treatment is achieved by stricter working conditions, but if necessary a carrier which is more acidic, for example a carrier with 60 to 90 wt .- ^ SiO ₂ and 10 to 40 wt .- ^ Al ₂ O ₅ or

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with 85 to 95 wt. $ Al ₂ O ₅ and 5 to 15 wt. # F or Cl can be used.

The exact choice and number of "heavier fractions treated" depends on the VI improvement required. The higher the VI improvement, the greater the decrease in viscosity. Preferably at least a portion of "vacuum residue" is used in process (2). Vacuum distillate and / or residue fractions can be used in process of type (1).

The term "viscosity index" as used herein is it is the viscosity index measured according to ASTM D 2270/64.

Apart from a certain breakdown to products that boil below 350 C, a conversion of sulfur and nitrogen compounds into HpS and ML can take place. At least the latter is expediently removed from a gas that is circulated, for example, by washing with water. Maintenance) boiling at 35O ° C
tion removed.

Products which boil at 35O ° C are expediently

The product of the hydrocatalytic VI improvement becomes then dewaxed with solvents and dewaxed. The heavier product fractions usually have pour points from -18 ° to -9 ° C, which can be achieved effectively and economically with solvents. By dewaxing with solvents, the microcrystalline wax present in these heavier fractions also becomes lighter than removed by catalytic dewaxing.

Suitable solvents are alkyl ketones with identical or different alkyl radicals with 1 "to 4 carbon atoms. Preferred methyl ethyl ketone and methyl isobutyl ketone are used as solvents and mixtures of these compounds. Aromatics such as benzene or toluene can also be present, where their amount preferably $ 25 to $ 75 (w / v) of the

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total solvent ". C ₁ -C chlorohydrocarbons, for example methylene chloride and ethylene dichloride, and Cp-Cg alkanes, in particular propane, are also suitable as solvents.

The oil is mixed with the solvent and usually heated to ensure complete dissolution and then cooled to precipitate the wax. The volume ratio of solvent to oil is 0.5 to 10: 1 ", and is preferably 1: 1 to 5:. 1, the mixture can be cooled to -5 ° to -30 ⁰ C. The cooling rate may be 0.5 to. 10 ° C / kinute and is preferably 2 ° to 7 ° C / minute.

N.

The precipitated wax is filtered off and the filter cake washed with cold solvent, the ratio being from solvent to oil is generally 0.2: 1 to 8: 1. The dewaxed oil is removed from the solvent by distillation freed. The solvent is recycled for reuse. Likewise, the precipitated wax can and the solvent used for washing is separated into product and solvent fractions by distillation will. . :

In the broadest sense, according to the invention, the feedstock is divided into two main streams, but one is another Subdivision possible, whereby a third stream only treats with solvents, a fourth stream only the Solvent dewaxing and possibly a fifth stream is subjected to an exclusively catalytic one Takes away. ;

Thus, the invention comprises the preparation of a range of lubricating oils by a process which is characterized in that an excess of 35O separating ⁰ C boiling petroleum fraction into at least one lighter fraction and at least two heavier fractions, the lighter fraction or the lighter fractions of a hydrocatalytic

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Dewaxing and dewaxing process and a solvent extraction to remove aromatics subjects at least one of the heavier fractions to one hydrocatalytic VI enhancement treatment and one Subjects to dewaxing and dewaxing process with a solvent and at least one more heavier one Fraction a solvent extraction process to remove aromatics and a dewaxing and dewaxing process Subjected with solvents.

Such a three-stream process is particularly suitable when products with both VI 75 to 100 and VI 101 to 150 should be made from the heavier fractions. The former is made from yours solely with solvents treated stream and the latter from the stream, that of the mixed treatment with catalysts and solvents was subjected, produced.

In another embodiment, the feedstock can be separated into three or more heavier fractions, at least one of which is a hydrocatalytic VI improvement process and a solvent dewaxing process, at least one further solvent extraction process for the removal of aromatics and a dewaxing process with solvents and at least one further a solvent dewaxing process without hydrocatalytic Subjected to VI improvement process or without solvent extraction process to remove aromatics will.

All product fractions or any product fraction can undergo a final treatment in a known manner may be subjected to improve color, resistance to oxidation or resistance to light. You can do this "treated with clay or bauxite, for example, or preferably a mild hydrocatalytic one known as" hydrofinishing " To be subjected to treatment. The need for these final treatments may be

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teren catalytically dewaxed and dewaxed fractions be less.

The method according to the invention can be carried out in a new lubricating oil plant or serve to expand an existing plant which consists of a solvent extraction unit and a solvent dewaxing unit. It has been found that adding two catalytic units to an existing plant consisting of two solvent treatment units reduces capital costs by up to 10% compared to adding two more solvent treatment units or one more solvent treatment unit and one catalytic unit. This advantage is in addition to the other advantages of flexibility, utilization of the individual processes in the most effective way and the possibility of oils from light oils with a viscosity of 22 cS at 38 ° C and a pour point of -4O ⁰ C to in a single plant to produce heavy oils with a viscosity of 1200 cS at 38 ⁰ C and a pour point of -12 C, achieved. I.

The invention will be described in connection with the figure which is a flow sheet of a lubricating oil manufacturing process represents according to the invention. The illustration is based on the expansion of an existing lubricating oil system, the existing system is indicated by hatching. I.

The system shown in the figure consists of two vacuum distillation columns 1 and 2, two propane deasphalting units 3, 4, a catalytic dewaxing unit 5, a catalytic hydrogenation unit 6, a Furfural extraction unit 7 and a solvent dewaxing unit 8th.

The residue of an atmospheric distillation with a boiling point

is through the I

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at the beginning of 250 ⁰ C, the vacuum lines 9 and IO

distillation column !! 1 and 2 supplied. Each column separates the atmospheric residue into ^{light ends boiling below 35O 0} C, which are drawn off overhead through lines 11 and 12 for other use, four distillation

1111

lat fractions A, B, C, D and A, B, C, D and a residue fraction E and E. The distillates A, B and C are through the lines 13 »14 and 15 of the catalytic dewatering unit 5 supplied. If necessary, can also

11 1

the distillates A, B and C wholly or partially of the catalytic dewaxing unit 5 through not shown Lines are fed. The catalytically dewaxed and dewaxed distillates then go to furfural extraction 7 and are represented by lines 16, 17 and 18 as

2 2 2
Products A, B and C deducted. Before the furfural extraction, the distillate fraction C is divided. A portion of this fraction separately goes through furfural extraction under different extraction conditions and then through line 19 for mixing with a stream described below. ,

The distillate D goes through line 20 (optionally together with the distillate D) to the catalytic hydrogenation and then for solvent dewaxing 8 and, after mixing with part of the distillate C from line 19 and a portion of the residue E withdrawn from line 30 as product D through line 21. The residue E goes through line 22 to propane deasphalting 3 and is then divided into three streams. Part goes through line 23 to the catalytic hydrogenation 6, part through line 24 for purpurol extraction 7, and a part looks around both units and goes directly to solvent dewaxing 8 through line 25 · The part going through line 23 is with Distillate D from line 20 is mixed and is so

2 possibly to a part of the product D. The one by line 24 going through the furfural extraction then goes to Solvent dewaxing, from which he is through line 26 as

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Product E ^ emerges. The through line 25 directly to

Part of the solvent dewaxing occurs as product E through line 27.

The residue E is through line 28 of the propane deasphalting 4, the catalytic hydrogenation 6 and the solvent dewaxing 8 and occurs through pipe

p
device 29 as product E. Part of this product is

as already mentioned, mixed with product D through line 30.

The invention is further illustrated by the following example.

example

A range of lubricating oils was made from an atmosphere residue of a Kuwait crude oil prepared according to the method described above and shown in the scheme. The types produced and the starting materials used are shown in Table 1 below.

Table 1 Type of lubricating oil starting material

.Transformer oil vacuum gas oil

2OS section A

33/100 section B

110/75 section C

22/125 section C

110/95 - $ 50 EAO, $ 50 cut D.

550/95 EAO

750/85 EAO

For these types, 2OS was a spindle oil with a viscosity of 4.1 cS at 99 ° C. For the other types, the first number means the ^{viscosity measured at 38 °} C. in cS and the second number means the viscosity index.

The starting materials were prepared by vacuum distillation of the atmospheric residue. The vacuum gas oil

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cut was taken overhead and had a boiling range of 210 ° "to 41O ⁰ C and a viscosity of 2.0 cS at 99 ⁰ O. The sections A, B, C and D were side streams had the following characteristics:

Section boiling range in TBP column viscosity

(determined by gas-liquid ο -u ^ QQ ⁰ C keitchromatography)

A 330-460 3.9

B 360-495 '6.1

C 350-580 9.4

D - 14.4

When using mixtures of the cuts, the proportions are given in vol .- ^ ö. The residue was treated with propane as Solvent deasphalted, a deasphalted oil (EAO) with a viscosity of 36.5 cS at 99 ° C. being obtained became.

The first four types of oil were made from the aforementioned starting materials produced by a combination of catalytic dewaxing and extraction with furfural. the catalytic dewaxing was carried out under the following conditions:

Temperature 320-40O ⁰ C

Pressure 69 bar (gauge pressure)

3 3 'circulation gas volume 1684 m / m

Room flow velocity, based on the liquid state 1.0 V / V / hour. '

Catalyst 0.5 wt .- ^ platinum on mordenite, the

decationized on a Fa-content of 0.75 wt .- ^ and for setting a Si0 ₂ / Al ₂ 0, - receives isses ^v from 18: had been acid treated. 1

The cycle gas was washed to increase the ELS content maximum 500 parts by volume HpS per million parts by volume at the reactor

gate outlet and the NH-z content to less than 5 parts by volume per million parts by volume.

The yields from the catalytic dewaxing and furfural treatment and the amount of furfural used are given in Table 2.

Table 2

Lubricating oil type transformer oil 2OS 33/100 110/75

Yield of dewaxed

Lubricating oil, wt .- ^ 70 82 82.5 80 hydrogen consumption,

/ m3 53.43_ 35.62 49.87 71.24

Yield of gas C ₁ -C ₁ -

Weight # ' ° 26.0 14.0 12.5 16.0

Yield of gasoline

C ₅ to 117 C, wt .- ^ 4.0 4.0 5.0 4.0

Purfurol extraction

Used furfural

amount, vol .-? 6 100 80 400 200

Extraction yield, wt .- ^ 55 75 48 68

The remaining four types of oil were made from the aforementioned starting materials produced by a combination of hydrogenation and solvent dewaxing. The hydrogenation was carried out under the following conditions:

Oil type Other 22/125 oil types

Temperature, ⁰ C 400-420 350-420

Pressure, bar 138 138

Circulation gas volume, nr / nr 1684 1250

Space flow velocity, on

Liquid state related, V / V / hour. 0.5 1.0

Catalyst 1.75 wt .- ^ Co and

12.7 wt. 56 Mo on silicon dioxide-aluminum oxide with a silicon content of the carrier of 9 wt. %

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The solvent dewaxing was carried out under the following conditions:

Temperature -12 ° to -18 ⁰ C

Solvent / oil ratio 6: 1 to 12: 1 solvent methyl isobutylene ketone

The yields from these processes are given in Table 3.

Table 3

Oil type 110/95 550/95 750/83 22/125

Hydrogenation data

Yield of waxy

term lubricating oil, wt. 81.0 90.7 96.0 47.0

Hydrogen consumption, Nm3 / _m 5

Gas yield, weight J &

Gasoline yield C _5-177 ⁰ C, 56 parts by weight yield of middle distillate 177-371 ⁰ C,

20th I. 3 500 1 330 2 · 11 50 5, 8th 3, 3 1, 4th 6th , 5 4, 5 0, 8th 0, 5 11 ,1 2, 6, 2, 36 , 6

Result of the
Dewaxing

Product yield, wt-56 83.5 83.5 83.5 75.0

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Claims (11)

Claims 1) A process for the simultaneous production of a number of different lubricating oils, characterized in that a ^{petroleum fraction boiling above 35O 0} C is separated into at least one lighter fraction and at least one heavier fraction, the lighter fraction or the lighter fractions partially or entirely in a hydrocatalytic dewaxing process and a solvent extraction to remove aromatics and the heavier fraction or the heavier fractions partially or completely subjected to a hydrocatalytic viscosity index improvement and a solvent dewaxing. 2) Method according to claim 1, characterized in that defines the intersection between the lighter and heavier fractions in the range of 450 ° to 500 ⁰ C. 3) Method according to claim 1 or 2, characterized in that the hydrocatalytic dewaxing is carried out ' leads by the lighter fraction or the lighter fractions together with hydrogen in a Temperature of 250 to 500 C and a pressure of 7 to 200 bar (manometer pressure) passes over a catalyst, the one or more incorporated into '"a crystalline mordenite with reduced alkali metal content Contains hydrogenation components from groups VIa and VIII of the periodic table. 4-) Process according to claim 1 to 3, characterized in that the hydrocatalytic dewaxing is carried out at a temperature of 265 to 43O ⁰ C, a pressure of 40 to 200 bar (manometer pressure), a room flow rate of 0.5 to 10 V / V /Hours. and with a water 409833/0786 material quantity from 900 to 2700 nr / m. 5) Method according to claim 1 or 2, characterized in that the solvent extraction with furfural at a solvent / oil volume ratio of 0.5: 1 performs and an average temperature of 15 ° to 150 ⁰ C 1 to fifth 6) Method according to claim 1 to 5, characterized in that the hydrocatalytic viscosity index improvement carried out by adding the heavier fraction or the heavier fractions together with hydrogen at a temperature of 3 ^ 0 to 460 C and one Pressure of 70 to 210 bar (manometer pressure) passes over a catalyst that contains one or more hydrogenation components from group VIa and / or VIII of the periodic table on a refractory oxide serving as a carrier contains. 7) Method according to claim 1 to 6, characterized in that the hydrocatalytic viscosity index improvement for the production of a dewaxed product with a Viskosi.tätindex of 75 to 100 at a temperature of 340 ° to 43O ⁰ C, a pressure of 70 to 170 bar ( Pressure gauge), a room flow velocity of 0.5 to 2 V / V / hour. and with a hydrogen quantity of 360 to 1800 m / m, 8) Method according to claim 1 to 6, characterized in that the hydrocatalytic viscosity index improvement for the production of a dewaxed product with a viscosity index of more than 100 at a temperature of 380 ° to 46O ⁰ C, a pressure of 120 to 210 bar (manometer pressure ), a room flow velocity of 0.2 to 2 V / V / hour. and with a hydrogen ■ 2 -2 amounts from 360 to 1800 m / m. 9) Method according to claim 1 to 8, characterized in that 409 8 3 3/0786 that the Lösungsraittelentwachsung using an alkyl ketone solvent at a solvent / oil ratio of 0.5: 1 is carried out and at a temperature of -5 ° to -30 ⁰ C: 1 to 10 degrees. 10) Method according to claim 1 or 2 for the simultaneous production of a number of different lubricating oils, thereby characterized in that a petroleum fraction boiling above 350 C is converted into at least one lighter one Fraction and at least two heavier fractions separates, the lighter fraction or the lighter ones Fractions of a hydrocatalytic dewaxing and a solvent extraction for the removal of aromatics, at least one of the heavier fractions a hydrocatalytic viscosity index improvement and a solvent dewaxing and at least one more heavy fraction solvent extraction to remove aromatics and solvent dewaxing subject. | 11) Method according to claim 10, characterized in that separating the starting material into three or more heavier fractions, at least one of these fractions a hydrocatalytic viscosity index improvement and a solvent dewaxing, at least one further of these fractions a solvent extraction to remove aromatics and a solvent dewaxing and at least one more of these fractions of solvent dewaxing without hydrocatalytic Subject to viscosity index improvement or without solvent extraction to remove aromatics. 409833/0786