CA1088447A - Process for the preparation of lubricating oil - Google Patents
Process for the preparation of lubricating oilInfo
- Publication number
- CA1088447A CA1088447A CA243,305A CA243305A CA1088447A CA 1088447 A CA1088447 A CA 1088447A CA 243305 A CA243305 A CA 243305A CA 1088447 A CA1088447 A CA 1088447A
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- Prior art keywords
- zone
- process according
- compounds
- hydrogen
- metals
- Prior art date
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A B S T R A C T
A process for the preparation of a lubricating oil with a low pour point, which comprises contacting in a first zone a substantially asphaltene-free waxy mineral oil fraction with a supported catalyst containing one or more metals (and/or compounds thereof) of Group VI and/or Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature of from 390-450°C, contacting in a second zone at least part of the liquid effluent of the first zone in the composition in which it becomes available, with an acidic sup-ported catalyst containing one or more metals (and/or compounds thereof) of Group VI and one or more non-noble metals (and/or compounds thereof) of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature between 350 and 390°C, and optionally dewaxing all or part of the effluent of the said second zone.
A process for the preparation of a lubricating oil with a low pour point, which comprises contacting in a first zone a substantially asphaltene-free waxy mineral oil fraction with a supported catalyst containing one or more metals (and/or compounds thereof) of Group VI and/or Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature of from 390-450°C, contacting in a second zone at least part of the liquid effluent of the first zone in the composition in which it becomes available, with an acidic sup-ported catalyst containing one or more metals (and/or compounds thereof) of Group VI and one or more non-noble metals (and/or compounds thereof) of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature between 350 and 390°C, and optionally dewaxing all or part of the effluent of the said second zone.
Description
~8447
2-The invention relates to a process for the preparation of a lubricating oil with a low pour point.
It is known to prepare lubricating oils by a two-step hydrotreatlng of deasphalted waxy mineral oil fractions~
followed by a dewaxing step. The yield of :Lubricating oil with a preset viscosity index often leaves to be desired.
It has now surprisingly been found that the yield of -~
lubricating oil which can be achieved, depends on a proper -~
choice of temperature and catalyst in the two steps, and on the use of the liquid effluent from the first hydro-treating step in the composition in which it becomes available as feed for the second hydrotreating step.
Acoordingly, the invention provides a process for the I preparation of a lubricating oil with a low pour point, ¦ 15 which comprises contacting in a firist zone a substantially ¦ asphaltene-free waxy mineral oil fraction with a supported catalyst containing one or more metals ~nd/or compounds - thereof) of Group VI and/or of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temper-ature of ~rom 390-450C, contacting in a seoond zone at least part of the liquid effluent of the first zone in the composition in which it becomes available, with an acidic supported catalyst containing one or more metals (and/or oompounds thereof) of Group VI and one or more non-noble metals ~and/or compounds thereof) of Group VIII of the Periodic Table of E1ementsg in the presence of hydrogen at t ~
;
~1088447 a temperature between 350 and 390C, and optionally dewaxing all or part of the effluent of the said second zone. ~-Suitable starting materials for the process according to the invention are high-boiling hydrocarbon mixtures, e.g., heavy petroleum fractions, and also heavy fractions obtained by pyrolysi~ of coal, bituminous shale or tar sand, which in the context of this invention are con-sidered to come within the term substantially asphaltene-free waxy mineral oil fraction. Petroleum fractions boilingat least in part above the boiling range of lubricating oil may be used to advantage. As feed ~or the present process use i8, preferab~, made of a distillate ~raction reoovered by vacuum distillation from a residual oil fraction obtained by atmospheric distillation. The boiling range of such a vacuum distillate is usually between 350C
and 550C. However, dea~phalted residual petroleum fractions may also be used.
The process according to the invention is carried out at ~levated temperature and pres~ure and in the presence of hydrogen or a hydrogen-containing gas in the first and second zones. Pure hydrogen may be used, but this is not necessary.
~ A gas with a hydrogen content of 70% or more by volume is i ~ perfectly suitable. In practice it will be preferable to use -.. . .
-' 25 a hydrogen-containing gas originating from a catalytic re-I forming plant. Such a gas not only has a high hydrogen content .
~; . ',:
. .
.
~0~8447 ~ .
- 4 - : -but also contains low-boiling hydrocarbonsl for example, methane, and a small quantity of propane. 1~
Pressures lower than 50 kg/cm2 in the first and the ~ -second zone are less desirable since they reduce the life .... .: . .:
of the catalysts while involving the risk of too high an aromatics content in the product, as a result of which ;-the viscosity index is adversely affected. A pressure above 250 kg/cm2 would require a very costly installation.
It is preferable to use a pressure between 100 and 200 kg/cm2.
!
The liquid hourly space velocity and the hydrogen/oil ratio may be selected between wide limits. It is pre~erred, however, to select a liquid hourly space velocity between :
0,1 and 10 kg o~ oil per hour per litre of catalyst. A
liquid hourly space velocity of less than 0.1 kg/hour per litre Or catalyst would require uneconomically large re-!: actors for a given degree of conversion, whereas a liquid ~;
hourly space velocity~of more than 10 kg per hour per i; .~ : . .
litre of catalyst would give only a low degree of conversion into the desired product. The hydrogen/oil ratio is, prefer- ;
ably, between 100 and 5,000 standard litres (litre~ at 1 bar and at 0C) per kg o~ oil. A very low H2/oil ratio would adversely affect the life o~ the catalyst, whereas ~ a very~high H2/oil ratio would cause a considerable 1099 ! :~ 25~ o;~pres6ure over~the~oatalyst beds, so that much energy~for ~ oompression would bé required for circulating the hydrogen-~
1 ~ ~ rich~gas~
.~ - , .. ..
--5- ; -,. :'~ ':
The support of the catalyst of the first zone may be ..
any refractory material. Suitable materials are, for ~
.; .
- example, alumina (aluminium oxide), silica (silicium oxide), magnesia (magnesium oxide), titanium oxide, zirconia (zirconium oxide), thoria (thorium oxide), boria (borium oxide) and mixtures and compounds of these metal oxides. It is preferred that the supports of the catalysts in the first an~ the second zone consist for the greater -part of alumina. Mixtures of alumina and silica, and in .. .
particular alumina and boria are very suitable. ~
.
In the first zone supported catalysts which contain one or more of the metals nickel, cobalt, molybdenum and tun~sten are very suitable, in particular catalysts which 1~ contain one of the metals nickel and cobalt and one of the 1 15 metals molybdenum and tungsten. A catalyst which consists of nickel and tungsten (or compounds, in particular oxides -., ~.
thereof) on an alumina/boria support i8 mostly preferred in ~-. 1 . . :: '. ' .
the first zone.
The presence of phosphorus and/or fluor in the catalyst in the ~rst zone is often of advantage.
~he amounts of the metals present in the catalyst in I the first zone may vary between wide limits. Very suitably j ~ the oatalyst contains from 10 to 30 parts by weight of a - Group VI~metal and~from 2 to 15 parts by weight Or a Group ~ ~ -25 ~ VIII metal per 100 parts of cataly~t.
~he metals in the fresh catalysts are very suitable in the oxidic form.
1 , , . ~ . .
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:
;~
1()88~47 ~-~
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The effluent of the first zone may be treated in order to remove therefrom undesired gaseous compounds, such as hydrogen sulphide (e.g., by adsorption of H2S in an aqueous amine solution, such as a solut~n of di-i~opropanolamine).
However, it is preferred to forward the total product emerging from the first zone into the second zone. -The preferred pressure, liquid hourly space velocity and hydrogen/oil ratio in the second zone are equal to those described for the firæt zone. The temperature of the second zone ~ould be between 350 and 390C; it should always be lower than the temperature of the first zone.
The cataly8t of the second zone should be an acidic ~upported catalysk. By the8e catalysts are meant those !I which, when adsorbing the indicator butter yellow (= di-; y C6H5 N=N-C6H4-N-(CH3)2~ and other still weaker basic indicators, show a colour change of these indioators, indicative of an acid medium.
:! - .
Suitable supports for the acidic supported cataly~ts are, for in~3tance, compounds of silica and alumina, such as 8ilica-alumina cracking catalysts, compounds o~ silica and zirconium dio~ide, compound8 of boron trioxide and alumina, compounds of boron trioxide and silica, compounds of alumina and halogen, such as alumina and fluorine or alumina, silica and fluorine, and the like.
The metal8 (or t;heir compounds) and comblnations thereof and the amounts thereof whioh are very suitable or preferred in the ,,'"
.~ .
:~ '" '' ' ' .~: ` .':
~8447 : ~;
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catalyst of the second zone are the same as those of the first zone. Very attractive catalysts for the second zone are nickel and tungsten (or compounds (e.g., oxides) there-of) on an alumina/boria support, and fluorinated nickel and tungsten (or compounds (e.g., oxides) thereof) on a silica-alumina carrier. -In many cases it will be attractive to use the same catalyst in the first and the second zone.
In case the pour point of the liquid effluent from the second zone is too high, this effluent may be dewaxed as such. However, it i9 preferred to remove therefrom lower boiling materials (e.g., by distillation) before dewaxing.
Very suitably all compounds which have a boiling point up to 400-450C are removed before dewaxing.
The dewaxing may be carried out in any desired manner, e.g., by mixing the liquid to be dewaxed with a suitable liquid (e.g , a mixture of methylethyl ketone and toluene), cooling the mixture to a temperature of about -20C and removing the solid wax.
It is preferred to carry out the dewaxing operation catalytically by oontacting the liquid to be dewaxed with a catalyst in the presence o~ hydrogen. Very suitable catalysts comprise one or more metals or compounds~ thereof .
of Group VI and VI~ of the Periodic Table supported on a j 25 cryatalline mordenite. As examples of very suitable metals may be mentioned platinum, palladium and tungsten. ~ ;
~: ' , :' : '~: ' ., .~ , .
~ '" " ' ~015184~7 ;. ':
Pressures of from 40-120 kg~cm2, temperatures of from ;-300-400C (in particular of from 300-350C~ and liquid hourly space velocities of from 0 1-2 kg oll per litre catalyst per hour are very suitable.
If desired,the effluent of the catalytic dewaxing may ~ ;
be topped in order to remove low-boiling constituents and/or extracted with a suitable extracting agent (e.g., sulphur dioxide, sulfolane) in order to remove aromatic constituents.
EXAMPLE
A waxy distillate having a boiling range of between 430C and 550C, obtained from a Middle East crude, was ' passed together with hydrogen over two con~ecutive cat,alyst I beds at a pressure of 140 kg/cm2, a liquid hourly ~pace velocity of 0.~ kg/l of oatalyst/hour, the hydrogen/oil ratio being 1750 Nl/kg.
The fir;3t reactor contained a catalyst having the fol- f lowing composition: :
Al23 57.5%; B203 - 6%; WO~ - 30%; NiO - 6 5`%
; ~ ~ The composition of the oatalyst in the second reactor -~, 20 was~
23 57-5%; B203 - 6%; W03 - 30%; NiO - 6 5%
In this particular ca~e the composition of the cataly~t ~ ;
in the second reactor;is therefore identical to that in the first reaotor. The temperatures of the two reactors vary, f ~;f~
. ., ., ~
25-~ a~d Table I shows the yield of oil with a viscosity index ' ~ of 95 t% by weight in relation to the total liquid effluent -f f `' ~ `` ` : :, :., ,; . ,.
'`` .'' ~:
8~447 : ~
':-': '.
g , ", , , . -, ,.
from the second reactor), obtained after topping at 430C~:
and after catalytic dewaxing of the said liquid effluent. :-The catalytic dewaxing was carried out by passing the . :
said liquid effluent (after topping at 430C) at a pressure of 60 kg/cm2, a liquid hourly space velocity of 0.5 kg/l of catalyst/hour, at a temperature of 315C, over a catalyst consisting of 10% by weight of tungsten (in r~
oxidic form) supported on a synthetic mordenite.
Similar experiments were carried out, the only dif-ference being the temperatures. ~ .
.
TABLE I
Temperature of 1st zone402 401 397 395 Temperature o~ 2nd zone320 340 360 370 Yield o~ oil, %w 5 51 52 58.5 Table I shows that the highest yields of oil with a viscosity index of 95 are obtained at a temperature of about 395C in the first reactor, while the temperature in the . :
seoond reactor lies between 360C and 390C; the yield diminishes as the temperature in the second reactor decreases. .
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''' ~:
. . .
.', .,`:, '' .
~, : .:
; ,, ' ' ' ' '.' , ,~ ' ;`, , ~ ~ ''`
':: :
It is known to prepare lubricating oils by a two-step hydrotreatlng of deasphalted waxy mineral oil fractions~
followed by a dewaxing step. The yield of :Lubricating oil with a preset viscosity index often leaves to be desired.
It has now surprisingly been found that the yield of -~
lubricating oil which can be achieved, depends on a proper -~
choice of temperature and catalyst in the two steps, and on the use of the liquid effluent from the first hydro-treating step in the composition in which it becomes available as feed for the second hydrotreating step.
Acoordingly, the invention provides a process for the I preparation of a lubricating oil with a low pour point, ¦ 15 which comprises contacting in a firist zone a substantially ¦ asphaltene-free waxy mineral oil fraction with a supported catalyst containing one or more metals ~nd/or compounds - thereof) of Group VI and/or of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temper-ature of ~rom 390-450C, contacting in a seoond zone at least part of the liquid effluent of the first zone in the composition in which it becomes available, with an acidic supported catalyst containing one or more metals (and/or oompounds thereof) of Group VI and one or more non-noble metals ~and/or compounds thereof) of Group VIII of the Periodic Table of E1ementsg in the presence of hydrogen at t ~
;
~1088447 a temperature between 350 and 390C, and optionally dewaxing all or part of the effluent of the said second zone. ~-Suitable starting materials for the process according to the invention are high-boiling hydrocarbon mixtures, e.g., heavy petroleum fractions, and also heavy fractions obtained by pyrolysi~ of coal, bituminous shale or tar sand, which in the context of this invention are con-sidered to come within the term substantially asphaltene-free waxy mineral oil fraction. Petroleum fractions boilingat least in part above the boiling range of lubricating oil may be used to advantage. As feed ~or the present process use i8, preferab~, made of a distillate ~raction reoovered by vacuum distillation from a residual oil fraction obtained by atmospheric distillation. The boiling range of such a vacuum distillate is usually between 350C
and 550C. However, dea~phalted residual petroleum fractions may also be used.
The process according to the invention is carried out at ~levated temperature and pres~ure and in the presence of hydrogen or a hydrogen-containing gas in the first and second zones. Pure hydrogen may be used, but this is not necessary.
~ A gas with a hydrogen content of 70% or more by volume is i ~ perfectly suitable. In practice it will be preferable to use -.. . .
-' 25 a hydrogen-containing gas originating from a catalytic re-I forming plant. Such a gas not only has a high hydrogen content .
~; . ',:
. .
.
~0~8447 ~ .
- 4 - : -but also contains low-boiling hydrocarbonsl for example, methane, and a small quantity of propane. 1~
Pressures lower than 50 kg/cm2 in the first and the ~ -second zone are less desirable since they reduce the life .... .: . .:
of the catalysts while involving the risk of too high an aromatics content in the product, as a result of which ;-the viscosity index is adversely affected. A pressure above 250 kg/cm2 would require a very costly installation.
It is preferable to use a pressure between 100 and 200 kg/cm2.
!
The liquid hourly space velocity and the hydrogen/oil ratio may be selected between wide limits. It is pre~erred, however, to select a liquid hourly space velocity between :
0,1 and 10 kg o~ oil per hour per litre of catalyst. A
liquid hourly space velocity of less than 0.1 kg/hour per litre Or catalyst would require uneconomically large re-!: actors for a given degree of conversion, whereas a liquid ~;
hourly space velocity~of more than 10 kg per hour per i; .~ : . .
litre of catalyst would give only a low degree of conversion into the desired product. The hydrogen/oil ratio is, prefer- ;
ably, between 100 and 5,000 standard litres (litre~ at 1 bar and at 0C) per kg o~ oil. A very low H2/oil ratio would adversely affect the life o~ the catalyst, whereas ~ a very~high H2/oil ratio would cause a considerable 1099 ! :~ 25~ o;~pres6ure over~the~oatalyst beds, so that much energy~for ~ oompression would bé required for circulating the hydrogen-~
1 ~ ~ rich~gas~
.~ - , .. ..
--5- ; -,. :'~ ':
The support of the catalyst of the first zone may be ..
any refractory material. Suitable materials are, for ~
.; .
- example, alumina (aluminium oxide), silica (silicium oxide), magnesia (magnesium oxide), titanium oxide, zirconia (zirconium oxide), thoria (thorium oxide), boria (borium oxide) and mixtures and compounds of these metal oxides. It is preferred that the supports of the catalysts in the first an~ the second zone consist for the greater -part of alumina. Mixtures of alumina and silica, and in .. .
particular alumina and boria are very suitable. ~
.
In the first zone supported catalysts which contain one or more of the metals nickel, cobalt, molybdenum and tun~sten are very suitable, in particular catalysts which 1~ contain one of the metals nickel and cobalt and one of the 1 15 metals molybdenum and tungsten. A catalyst which consists of nickel and tungsten (or compounds, in particular oxides -., ~.
thereof) on an alumina/boria support i8 mostly preferred in ~-. 1 . . :: '. ' .
the first zone.
The presence of phosphorus and/or fluor in the catalyst in the ~rst zone is often of advantage.
~he amounts of the metals present in the catalyst in I the first zone may vary between wide limits. Very suitably j ~ the oatalyst contains from 10 to 30 parts by weight of a - Group VI~metal and~from 2 to 15 parts by weight Or a Group ~ ~ -25 ~ VIII metal per 100 parts of cataly~t.
~he metals in the fresh catalysts are very suitable in the oxidic form.
1 , , . ~ . .
i, , - .:. .
:
;~
1()88~47 ~-~
.`. ., 6 -~
" . ~.
The effluent of the first zone may be treated in order to remove therefrom undesired gaseous compounds, such as hydrogen sulphide (e.g., by adsorption of H2S in an aqueous amine solution, such as a solut~n of di-i~opropanolamine).
However, it is preferred to forward the total product emerging from the first zone into the second zone. -The preferred pressure, liquid hourly space velocity and hydrogen/oil ratio in the second zone are equal to those described for the firæt zone. The temperature of the second zone ~ould be between 350 and 390C; it should always be lower than the temperature of the first zone.
The cataly8t of the second zone should be an acidic ~upported catalysk. By the8e catalysts are meant those !I which, when adsorbing the indicator butter yellow (= di-; y C6H5 N=N-C6H4-N-(CH3)2~ and other still weaker basic indicators, show a colour change of these indioators, indicative of an acid medium.
:! - .
Suitable supports for the acidic supported cataly~ts are, for in~3tance, compounds of silica and alumina, such as 8ilica-alumina cracking catalysts, compounds o~ silica and zirconium dio~ide, compound8 of boron trioxide and alumina, compounds of boron trioxide and silica, compounds of alumina and halogen, such as alumina and fluorine or alumina, silica and fluorine, and the like.
The metal8 (or t;heir compounds) and comblnations thereof and the amounts thereof whioh are very suitable or preferred in the ,,'"
.~ .
:~ '" '' ' ' .~: ` .':
~8447 : ~;
.i.....
,,~
catalyst of the second zone are the same as those of the first zone. Very attractive catalysts for the second zone are nickel and tungsten (or compounds (e.g., oxides) there-of) on an alumina/boria support, and fluorinated nickel and tungsten (or compounds (e.g., oxides) thereof) on a silica-alumina carrier. -In many cases it will be attractive to use the same catalyst in the first and the second zone.
In case the pour point of the liquid effluent from the second zone is too high, this effluent may be dewaxed as such. However, it i9 preferred to remove therefrom lower boiling materials (e.g., by distillation) before dewaxing.
Very suitably all compounds which have a boiling point up to 400-450C are removed before dewaxing.
The dewaxing may be carried out in any desired manner, e.g., by mixing the liquid to be dewaxed with a suitable liquid (e.g , a mixture of methylethyl ketone and toluene), cooling the mixture to a temperature of about -20C and removing the solid wax.
It is preferred to carry out the dewaxing operation catalytically by oontacting the liquid to be dewaxed with a catalyst in the presence o~ hydrogen. Very suitable catalysts comprise one or more metals or compounds~ thereof .
of Group VI and VI~ of the Periodic Table supported on a j 25 cryatalline mordenite. As examples of very suitable metals may be mentioned platinum, palladium and tungsten. ~ ;
~: ' , :' : '~: ' ., .~ , .
~ '" " ' ~015184~7 ;. ':
Pressures of from 40-120 kg~cm2, temperatures of from ;-300-400C (in particular of from 300-350C~ and liquid hourly space velocities of from 0 1-2 kg oll per litre catalyst per hour are very suitable.
If desired,the effluent of the catalytic dewaxing may ~ ;
be topped in order to remove low-boiling constituents and/or extracted with a suitable extracting agent (e.g., sulphur dioxide, sulfolane) in order to remove aromatic constituents.
EXAMPLE
A waxy distillate having a boiling range of between 430C and 550C, obtained from a Middle East crude, was ' passed together with hydrogen over two con~ecutive cat,alyst I beds at a pressure of 140 kg/cm2, a liquid hourly ~pace velocity of 0.~ kg/l of oatalyst/hour, the hydrogen/oil ratio being 1750 Nl/kg.
The fir;3t reactor contained a catalyst having the fol- f lowing composition: :
Al23 57.5%; B203 - 6%; WO~ - 30%; NiO - 6 5`%
; ~ ~ The composition of the oatalyst in the second reactor -~, 20 was~
23 57-5%; B203 - 6%; W03 - 30%; NiO - 6 5%
In this particular ca~e the composition of the cataly~t ~ ;
in the second reactor;is therefore identical to that in the first reaotor. The temperatures of the two reactors vary, f ~;f~
. ., ., ~
25-~ a~d Table I shows the yield of oil with a viscosity index ' ~ of 95 t% by weight in relation to the total liquid effluent -f f `' ~ `` ` : :, :., ,; . ,.
'`` .'' ~:
8~447 : ~
':-': '.
g , ", , , . -, ,.
from the second reactor), obtained after topping at 430C~:
and after catalytic dewaxing of the said liquid effluent. :-The catalytic dewaxing was carried out by passing the . :
said liquid effluent (after topping at 430C) at a pressure of 60 kg/cm2, a liquid hourly space velocity of 0.5 kg/l of catalyst/hour, at a temperature of 315C, over a catalyst consisting of 10% by weight of tungsten (in r~
oxidic form) supported on a synthetic mordenite.
Similar experiments were carried out, the only dif-ference being the temperatures. ~ .
.
TABLE I
Temperature of 1st zone402 401 397 395 Temperature o~ 2nd zone320 340 360 370 Yield o~ oil, %w 5 51 52 58.5 Table I shows that the highest yields of oil with a viscosity index of 95 are obtained at a temperature of about 395C in the first reactor, while the temperature in the . :
seoond reactor lies between 360C and 390C; the yield diminishes as the temperature in the second reactor decreases. .
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. . .
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~, : .:
; ,, ' ' ' ' '.' , ,~ ' ;`, , ~ ~ ''`
':: :
Claims (11)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOS:
1. A process for the preparation of a lubricating oil with a low pour point, which comprises contacting in a first zone a substantially asphaltene-free waxy mineral oil fraction with a supported catalyst contain-ing one or more metals (and/or compounds thereof) of Group VI and/or Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature of from 390-450°C, contacting in a second zone at least part of the liquid effluent of the first zone in the composition in which it becomes, available, with an acidic supported catalyst containing one or more metals (and/or compounds thereof) of Group VI and one or more non-noble metals (and/
or compounds thereof) of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature between 350 and 390°C, and optional.
ly dewaxing all or part of the effluent of the said second zone.
or compounds thereof) of Group VIII of the Periodic Table of Elements, in the presence of hydrogen at a temperature between 350 and 390°C, and optional.
ly dewaxing all or part of the effluent of the said second zone.
2. A process according to claim 1, in which the supports in the first and second zone consist for the greater part of alumina.
3. A process according to claim 1, in which the supports in the first and second zone comprise boria.
4. A process according to claim 1, 2 or 3, in which the catalysts in the first and second zone comprise compounds of nickel and tungsten.
5. A process according to claim 1, 2 or 3, in which the catalysts in the first zone and the second zone are identical.
6. A process according to claim 1, in which the pressure in the first and second zone is between 100 and 200 kg/cm2.
7. A process according to claim 1, in which the total liquid ef-fluent of the first zone is contacted with the catalyst in the second zone.
8. A process according to claim 1, in which the dewaxing is car-ried out catalytically in the presence of hydrogen with the aid of a morde-nite.
9. A process according to claim 8, in which the mordenite con-tains one or more non-noble metals of Group VIII of the Periodic Table of Elements.
10. A process according to claim 9, in which the mordenite con-tains tungsten.
11. A process according to any one of claims B, 9 or 10, in which the catalytic dewaxing is carried out at a pressure of from 40-120 kg/cm2, a temperature of from 300-400°C and a liquid hourly space velocity of from 0.1-2 kg oil per litre catalyst per hour.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA243,305A CA1088447A (en) | 1976-01-12 | 1976-01-12 | Process for the preparation of lubricating oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA243,305A CA1088447A (en) | 1976-01-12 | 1976-01-12 | Process for the preparation of lubricating oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1088447A true CA1088447A (en) | 1980-10-28 |
Family
ID=4104955
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA243,305A Expired CA1088447A (en) | 1976-01-12 | 1976-01-12 | Process for the preparation of lubricating oil |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1088447A (en) |
-
1976
- 1976-01-12 CA CA243,305A patent/CA1088447A/en not_active Expired
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