CA2320106A1 - Process for improving basestock low temperature performance using a combination catalyst system - Google Patents
Process for improving basestock low temperature performance using a combination catalyst system Download PDFInfo
- Publication number
- CA2320106A1 CA2320106A1 CA002320106A CA2320106A CA2320106A1 CA 2320106 A1 CA2320106 A1 CA 2320106A1 CA 002320106 A CA002320106 A CA 002320106A CA 2320106 A CA2320106 A CA 2320106A CA 2320106 A1 CA2320106 A1 CA 2320106A1
- Authority
- CA
- Canada
- Prior art keywords
- component
- zsm
- catalyst
- dimethylcyclopentane
- feed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Abstract
Waxy feeds are converted to a basestock using a unitized mixed powdered pellet catalyst comprising a metal hydrogenation component on a support having a first dewaxing component and a second isomerization component, wherein the first component is selected from 10 and 12 ring molecular sieves and mixtures thereof and the second component is an amorphous inorganic oxide. The first and second components are present in a ratio sufficient to promote wax isomerization and naphthene distractions without substantial decrease in VI.
Description
PROCESS FOR llvvIPROVIrTG BASESTOCK LOW TEMPERATURE
PERFORMANCE USING A COMBINATION CATALYST SYSTEM
FIELD OF TIC 1)VVENTION
This invention relates to the hydrodewaxing of waxy feeds includ-ing slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate, waxy raffnates, and waxy distillates to produce a Tube oil basestock or blending stock. More specifically, this invention relates to the conversion of a waxy feed using a mixed catalyst capable of promoting wax isomerization and naphthene destruction to form a Tube basestock with minimum VI loss and having good low temperature properties.
BACKGROUND OF THE INVENTION
The performance criteria for lubricants such as those used in automatic transmission fluids and passenger car engine oils has become increasingly more severe with users requiring basestock that provide better wear protection, improved volatility and low temperature properties.
Waxy feeds can be converted to liquid products using well known catalytic dewaxing catalysts; however, in these instances the selective cracking of para~ns typically results in a loss of viscosity index (Vl7 which is undesir-able.
In contrast, isomerization of waxy feeds using molecular sieve based catalyst that have linear 1D pore structures produces Tube basestocks without loss in VI. While this isomerization process offers benefits over that of catalytic dewaxing there nonetheless remains a need for different and improved processes for converting waxy feeds to lobe basestocks without significant loss in VI and which basestock has good low temperature properties.
SU~N1ARY OF THE INVENTION
This invention relates to a method for the hydrodewaxing of feeds to produce a Tube basestock having improved low temperature properties which comprises: contacting the feed with a unitized mixed powder pellet catalyst under hydrodewaxing conditions, the catalyst comprising a metal hydrogenation component on a support having a first dewaxing component and a second isomerization component, wherein the first component is selected from 10 and 12 ring molecular sieves and mixtures thereof and the second component is an amorphous inorganic oxide and wherein the first and second components are present in a ratio such that when evaluated in the conversion of methyl cyclo-hexane at 320°C to 1,1-dimethylcyclopentane, 1,2-dimethylcyclopentane, 1,3-dimethylcyclopentane and ethylcyclopentane, the catalyst will provide a traps-1,2-/traps-1,3-dimethylcyclopentane in the range of at least 1, and a selectivity to ethylcyclopentane, at 10% conversion, of at least about 50%.
This and other embodiments of the invention will be discussed below.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic drawing showing the conversion of methylcyclohexane to various cyclopentane compounds at 320°C.
Figure 2 is a graph showing Brookfield viscosity vs. yield for various catalyst mixtures.
PERFORMANCE USING A COMBINATION CATALYST SYSTEM
FIELD OF TIC 1)VVENTION
This invention relates to the hydrodewaxing of waxy feeds includ-ing slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate, waxy raffnates, and waxy distillates to produce a Tube oil basestock or blending stock. More specifically, this invention relates to the conversion of a waxy feed using a mixed catalyst capable of promoting wax isomerization and naphthene destruction to form a Tube basestock with minimum VI loss and having good low temperature properties.
BACKGROUND OF THE INVENTION
The performance criteria for lubricants such as those used in automatic transmission fluids and passenger car engine oils has become increasingly more severe with users requiring basestock that provide better wear protection, improved volatility and low temperature properties.
Waxy feeds can be converted to liquid products using well known catalytic dewaxing catalysts; however, in these instances the selective cracking of para~ns typically results in a loss of viscosity index (Vl7 which is undesir-able.
In contrast, isomerization of waxy feeds using molecular sieve based catalyst that have linear 1D pore structures produces Tube basestocks without loss in VI. While this isomerization process offers benefits over that of catalytic dewaxing there nonetheless remains a need for different and improved processes for converting waxy feeds to lobe basestocks without significant loss in VI and which basestock has good low temperature properties.
SU~N1ARY OF THE INVENTION
This invention relates to a method for the hydrodewaxing of feeds to produce a Tube basestock having improved low temperature properties which comprises: contacting the feed with a unitized mixed powder pellet catalyst under hydrodewaxing conditions, the catalyst comprising a metal hydrogenation component on a support having a first dewaxing component and a second isomerization component, wherein the first component is selected from 10 and 12 ring molecular sieves and mixtures thereof and the second component is an amorphous inorganic oxide and wherein the first and second components are present in a ratio such that when evaluated in the conversion of methyl cyclo-hexane at 320°C to 1,1-dimethylcyclopentane, 1,2-dimethylcyclopentane, 1,3-dimethylcyclopentane and ethylcyclopentane, the catalyst will provide a traps-1,2-/traps-1,3-dimethylcyclopentane in the range of at least 1, and a selectivity to ethylcyclopentane, at 10% conversion, of at least about 50%.
This and other embodiments of the invention will be discussed below.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic drawing showing the conversion of methylcyclohexane to various cyclopentane compounds at 320°C.
Figure 2 is a graph showing Brookfield viscosity vs. yield for various catalyst mixtures.
DESCRIPTION OF THE IZ~1VENTION
The feed suitable in the practice of the present invention includes waxy hydrocarbon oils such as slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate, waxy raffmates and waxy distillates.
Typically, such feeds will have wax contents of 15% or more. The preferred feed will have a nitrogen and sulfilr content each below about 20 wppm by weight. Indeed, if the feed contains higher amounts of sulfur and nitrogen, the feed can be first subjected to hydrotreating under typical hydrotreating condi-tions to reduce the sulfur and nitrogen contents. Any of the conventional hydro-treating catalysts can be employed like Ni/Mo on alumina, Ni/W on alumina Co/Mo on alumina. In other words any of the Group VIB to Group VIII and mixtures thereof (the metal groups referred to here and hereinafter are those metals of the Periodic Table of Elements; Sargent-Welch Scientific Co.) on metal oxide refractory supports may be employed. Commercial examples of such are identified as HDN-30 and KF-840.
Hydrotreating is conducted so as to lower the sulfur and nitrogen contents to levels of 20 ppm or less nitrogen or 20 ppm or less sulfur especially ppm less nitrogen and 10 ppm or less sulfur and most preferably to levels below 5 ppm for nitrogen and 5 ppm or less for sulfur.
Waxy feeds secured from natural petroleum sources contain quantities of sulfur and nitrogen compounds which are known to deactivate wax hydroisomerization catalysts. To prevent this deactivation it is preferred that the feed contain no more than 10 ppm sulfur, preferably less than 2 ppm sulfur and no more than 2 ppm nitrogen, preferably less than 1 ppm nitrogen.
The feed suitable in the practice of the present invention includes waxy hydrocarbon oils such as slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate, waxy raffmates and waxy distillates.
Typically, such feeds will have wax contents of 15% or more. The preferred feed will have a nitrogen and sulfilr content each below about 20 wppm by weight. Indeed, if the feed contains higher amounts of sulfur and nitrogen, the feed can be first subjected to hydrotreating under typical hydrotreating condi-tions to reduce the sulfur and nitrogen contents. Any of the conventional hydro-treating catalysts can be employed like Ni/Mo on alumina, Ni/W on alumina Co/Mo on alumina. In other words any of the Group VIB to Group VIII and mixtures thereof (the metal groups referred to here and hereinafter are those metals of the Periodic Table of Elements; Sargent-Welch Scientific Co.) on metal oxide refractory supports may be employed. Commercial examples of such are identified as HDN-30 and KF-840.
Hydrotreating is conducted so as to lower the sulfur and nitrogen contents to levels of 20 ppm or less nitrogen or 20 ppm or less sulfur especially ppm less nitrogen and 10 ppm or less sulfur and most preferably to levels below 5 ppm for nitrogen and 5 ppm or less for sulfur.
Waxy feeds secured from natural petroleum sources contain quantities of sulfur and nitrogen compounds which are known to deactivate wax hydroisomerization catalysts. To prevent this deactivation it is preferred that the feed contain no more than 10 ppm sulfur, preferably less than 2 ppm sulfur and no more than 2 ppm nitrogen, preferably less than 1 ppm nitrogen.
To achieve these limits the feed is preferably hydrotreated to reduce the sulfur and nitrogen content.
Hydrotreating can be conducted using any typical hydrotreating catalyst such as Ni/Mo on alumina, Co/Mo on alumina, ColNi/Mo on alumina, e.g., KF-840, KF-843, HDN-30, HDN-60, Criteria C-411, etc. Similarly, bulk catalysts comprising Ni/Mn/Mo or Cr/Ni/Mo sulfides as described in U.S. Patent 5,122,258 can be used.
Hydrotreating is performed at temperatures in the range 280°C to 400°C, preferably 340°C to 380°C at pressures in the range 500 to 3000 psi, hydrogen treat gas rate in the range of 500 to 5000 SCF/bbl and a flow velocity in the range 0.1 to 5 LHSV, preferably 1 to 2 LHSV.
The hydrotreated waxy oil is stripped to remove ammonia and H2S
and then is subjected to the hydrodewaxing process of the present invention.
The catalyst employed in the hydrodewaxing of waxy feeds in accordance with the present invention is a unitized mixed powdered pellet catalyst. The term "unitized" as used here and in the claims means that each pellet is one made by mixing together a powdered first catalytic component with a powdered second catalytic component and pelletizing the mixture to produce pellets each of which contain all of the powder components previously recited.
The unitized catalyst can be prepared by starting with individual f nished catalysts, pulverizing and powdering such individual finished catalysts, mixing the powdered materials together to form a homogeneous mass, then compressing/extruding and pelleting thus producing the unitized pellet catalysts comprising a mixture of the individual, different, and distinct catalyst components. Pulverizing and powdering is to a consistency achievable using a mortar and pestle or other such conventional powdering means.
The catalyst used in the process of the present invention comprises a metal hydrogenation component on a two component support. The metal hydrogenation component is at least one of a Group VIB or Group VIII metal, preferably a Group VIII metal, and more preferably Pt or Pd. The metal is dispersed on at least one of the first and second components of the support, and preferably on both components. Typically the metal will be present in an amount ranging from about 0.1 to about 30 wt%, and preferably about 0.1 to IO wt%. If the metal is a Group VIII noble metal, then the preferred amount is 0.1 to 5 wt%. The catalyst may also include a substantially inert binder or matrix material.
The first component is a catalytic dewaxing component including crystalline 10 and 12 ring molecular sieves. Crystalline molecular sieves include metallo-, e.g., alumino silicates, alumino phosphates and silicoalumino-phosphates. Examples of crystalline alumino silicates include zeolites, e.g., ZSM-5, ZSM-11, ZSM-12, Theta-1 (ZSM-22), ZSM-23, ZSM-35, ZSM-48 natural and synthetic ferrierites, ZSM-57, Beta Mordenite and Offretite.
Examples of crystalline alumino and silicoalumino-phosphates include SAPO-11, SAPO-41, SAPO-31, MAPO-11 and MAPO-31. Preferred include ZSM-5, ZSM-22, ZSM-23, ferrierites, and SAPO-11.
The second isomerization component can be any of the typical isomerization catalyst such as those comprising amorphous refractory metal oxide support base (e.g., alumina, silica alumina, zirconia, titania, etc.) on which has been preferably deposited a catalytically active metal selected from Group VI B, Group VII B, Group VIII metals and mixtures thereof, preferably Group VIII, more preferably noble Group VIII, most preferably Pt or Pd and optionally including a promoter or dopant such as halogen, phosphorus, boric, yttria, rare earth oxides, from e.g., La, Ce, etc., magnesia, etc. preferably halogen, yttria or magnesia, most preferably fluorine. The catalytically active metals are present in the range 0.1 to 5 wt%, preferably 0.1 to 3 wt%, more preferably 0.1 to 2 wt%, most preferably 0.1 to 1 wt%. The promoters and dopants are used to control the acidity of the isomerization catalyst. Thus, when the isomerization catalyst employs a base-material such as alumina, acidity is imparted to the resultant catalyst by addition of a halogen, preferably fluorine. When a halogen is used, preferably fluorine, it is present in an amount in the range 0.1 to 10 wt%, prefer-ably 0.1 to 3 wt%, more preferably 0.1 to 2 wt%, most preferably 0.5 to 1.5 wt%. Similarly, if silica-alumina is used as the base material, acidity can be controlled by adjusting the ratio of silica to alumina or by adding a dopant such as yttria, rare earth oxides, from, e.g., La, Ce, etc., boric or magnesia which reduces the acidity of the silica-alumina base material as taught on U.S.
Patent 5,254,518 (Soled, McVicker, Gates, Miseo).
The first and second components are combined in a ratio sufficient to promote wax isomerization and napthene destruction without substantial decrease in VI. The zeolite to amorphous inorganic oxide ratios for catalysts according to the invention range from about 1:1 to 1:20 by weight, subject to the MC~I test described below.
One technique for determining the proper ratio of first and second components in the catalyst is based on an evaluation of the combined components containing about 0.5 wt% Pt in converting methylcyclohexane (MCP to various cyclopentane compounds. Catalyst that at 320°C provide a ratio of traps-1,2-dimethylcyclopentane to traps-1,3-dimethylcyclopentane (traps-l,2/trans-1,3 DMCP) in the range of at least one have been found to promote wax isomerization and naphathene destruction of feeds without substantial decrease in VI.
The second factor is when the catalyst, impregnated with about 0.5 wt% Pt and evaluated in converting methylcyclohexane (MCH) to various cyclopentane compounds at 10% conversion, exhibits a selectivity for ethyl-cyclopentane (ECP) formation above at least 50%.
This technique is fiuther explained as follows. The reaction of MCH over the catalyst to various cyclopentane products is shown in Figure 1.
As indicated in Figure 1, the products of MCH decomposition include ethyl-cyclopentane, cis- and traps-1,2-dimethylcyclopentane, cis- and traps-1,3-dimethylcyclopentane and 1,1 dimethylcyclopentane. This technique, also known as the MCH test is used to define relative acid site concentration, strengths and active site constraint for the catalysts according to the invention.
The key factors are summarized as follows: (1) total conversion of MCH for a given catalyst weight at 320°C is an indication of the relative number of acid sites; (2) selectivity to ECP, at 10% conversion, is a measure of the relative acid strength wherein high ECP selectivity values indicates low acid strength and low ECP selectivity values indicates high acid strength; and (3) the ratio of traps-1,2-DCMP to traps-1,3-DCMP correlates with the constraint at the catalyst active site wherein a high ratio (> 1 ) indicates little or no physical constraint at the active site and a low ratio (<1) indicates a physical constraint at the active site.
In the present process, to produce a catalyst that will give improved low temperature properties, the ratio of traps-1,2-DCMP to traps-1,3-DCMP is adjusted to from 1:1 to 2:1 predominately by controlling the acid _g_ strength of the amorphous isomerization component. It is preferred to use higher acid strength amorphous components such as silica-alumina.
Conversely, a catalyst that will give high yield is produced by decreasing the acid strength of the amorphous phase. In this case it is preferred to use lower acid strength amorphous components such as alumina. Another way of making such a catalyst is by changing the ratio of the microporous component to the amorphous component such that the unitized catalyst has a traps-1,2 traps-1,3 DMCP ratio of less than 1.
The hydrodewaxing process utilizing the catalyst of the present invention is conducted at temperatures between about 200°C to 400°C, prefer-ably 250°C to 380°C and most preferably 300°C to 350°C at pressures between about 500 to 5,000 psig (3.55 to 34.6 mPa), preferably 1,000 to 2000 psig (7.0 to 13.9 mPa), a hydrogen gas treat ratio of 500 to 10000 SCF H2B (89 to 1780 m3/m3), preferably 2,000 to 5,000 SCF HZB (356 to 890 m3/m3) and a LHSV
of 0.5 to 5 v/v/hr, preferably 1 to 2 v/v/hr.
In an alternate embodiment of the present invention the feed is first subject to solvent dewaxing to a pour point on the order of +10°C or lower.
The dewaxing solvent used may include the C3-C6 ketones such as methyl ethyl ketone (MEK), methyl isobutyl ketone (NIIBK), mixtures of MEK
and MIBK, aromatic hydrocarbons like toluene, mixtures of ketones and aromatics like MEK/toluene, ethers such as methyl t-butyl ethers and mixtures of same with ketones or aromatics. Similarly, liquefied, normally gaseous hydro-carbons like propane, propylene, butane, butylene, and combinations thereof may be used as the solvent. Preferably the solvent employed will be an equal _g_ volume mixture of methyl ethyl ketone and methyl isobutyl ketone. Typically the isomerate to solvent ratio will range between 1 to 10 and preferably will be about 1:3. The dewaxed feed is then subjected to hydrodewaxing as described hereinabove.
The present invention is demonstrated below in the non-limiting examples.
EXAMPLES
Comparative Example 1 A catalyst (B) comprising 0.5 wt% Pt ZSM-5 (silica/alumina ratio 220:1) and alumina in the weight ratio of 25:75, was used in two runs to dewax a hydrocrackate distillate having the following properties:
KV, cSt at 100°C 3.808 KV, cSt at 135°C 2.28 Pour Point, °C 39 Boiling Range (GCD) 325-503°C
The dewaxing conditions employed are listed in the accompanying Table. The results are shown in column B of the Table following Example 2.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 40 and a trans-1, 2/trans-1,3 dimethylcylopentane ratio of 0.02 as shown in the Table. A comparison of columns A and B of the Table shows that the VI of the resulting liquid product (350°C+) was lower than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brool~eld Viscosity at -40°C
(additized with a standard Ford type ATF adpack), are also shown in the Table. The Brookfield Viscosity is reduced by catalytic dewaxing over that of a solvent dewaxed product. However, the Brookfield Viscosities of both solvent and cat dewaxed products are very poor.
Comparative Example 2 A catalyst (C) comprising 0.5 wt% Pt ZSM-5 (silicalalumina ratio 220:1) and silica-alumina in the weight ratio of 50:50, was used to dewax a hydrocrackate distillate having the properties noted in Comparative Example 1.
This catalyst was made by combining the powdered ZSM-S (Si/Al ratio 110) with the powdered amorphous component in the weight ratio of 50:50 and then loading platinum by incipient wetness using platinum tetraamine dichloride.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 47 and a traps-1, 2/trans-1,3 dimethylcylopentane ratio of 0.82 as shown in the Table following Example 2.
A comparison of columns A and C, in the Table shows that the VI of the resulting liquid product (350°C+) was lower than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brool~ield Viscosity -40°C (additized with a standard Ford type ATF adpack), are also shown in the Table. The Brookfield Viscosity is reduced by catalytic dewaxing over that of a solvent dewaxed product but not significantly over that obtained using the alumina bound catalyst in Example 1.
Example 1 A catalyst (D) comprising 0.5 wt% Pt ZSM-5 (silica/alumina ratio 220:1) and silica alumina in the weight ratio of 10:90, was used to dewax a hydrocrackate distillate having the properties noted in Comparative Example 1.
This catalyst was made by combining the powdered ZSM-5 (Si/Al ratio 110) with the powdered amorphous component in the weight ratio of 10:90 respectively and then loading platinum by incipient wetness using platinum tetraamine dichloride.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 50 and a traps-1,2/trans-1,3 dimethylcylopentane ratio of 1.80 as shown in the Table following Example 2.
Both of these values are within the criteria for catalysts of this invention.
A
comparison of columns A and D, in Table 1 shows that the VI of the resulting liquid product (350°C+) w~ lugher than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brookfield Viscosity at -40°C (addized in a standard ECA/ATF adpack), are also shown in the Table.
The Brookfield Viscosity is significantly reduced by catalytic dewaxing with this catalyst over that of a solvent dewaxed product in the Table 1.
Example 2 The procedure of Example 1 was followed using 0.5 wt% on Pt on theta-1 (TON) on silica-alutnina (Catalyst E)and 0.5 wt% Pt on A1203 in the weight ratio of 25:75 (Catalyst F-Comparative). Theta-1 is a 10 ring zeolite and is described in EP 057049. This catalyst was made by combining the powdered TON zeolite (Si/Al ratio 30) with the powdered amorphous component in different ratios and then loading platinum by incipient wetness using platinum tetraamine dichloride. The condition and results are set out in columns E and F
of Table 1.
~
N 'n O ~ .-. ~ ~ ~ N
en ...~ .-. ~ ~ Oy l~ r., ...r ~ O ....
~'y M ." N M .-. ' ~ N C
~
N
v.r ~ tef M
p~ v1 ... N 'n x, .-~ v1 .-, N 00 .-.
w ~ ~ ~ ~ N ~ M ~~r ' ,~." ~ r";
H
'b ~
M ~ 00 M g v.r M ~ M l~ ~' M N
.-w .--~
A
N $ "", N 0M0~ M ~ N .-N, 10 00 M ~", N M ~ ,.., , N ...:
O
~-~ O ~ N O O 0~0 O M
M ~ ~. ~ .-' h U ~ a E
N ' O o0 " N M v0 N
.-' ~ ..w ~ h N ~ ~ 00 M ,~ N ~ ~ ~ ' pp "", C
~_ ~ h ~ O M
M h ~' N rr , N
N
N a ~ .~ g N o ~ o ~ g ~ O o ~a M ~ N ~~~,~ , ~ ~~o "'~~°°N ° ~~z d ~ M CO ~. , n U
° U U
o ~ °
..~. OV .~~~r' N M
w o U .a .~ ~ U o ..
o z ~ ~w ~ ~a~~ °
-~ V v Or~4 ~ ~ E..~~?~ ~~ ~ ~V o s ~pG+.~.~ ~° ~°vO, ~
0 0 ~ .~ .N o V ~~Hw >H ~~M»~a, ~p~., ~Uw~A
The results shown in the Table are further illustrated in Figure 2 which is a graph showing Brool~eld viscosity vs. yield for various catalyst combinations.
Hydrotreating can be conducted using any typical hydrotreating catalyst such as Ni/Mo on alumina, Co/Mo on alumina, ColNi/Mo on alumina, e.g., KF-840, KF-843, HDN-30, HDN-60, Criteria C-411, etc. Similarly, bulk catalysts comprising Ni/Mn/Mo or Cr/Ni/Mo sulfides as described in U.S. Patent 5,122,258 can be used.
Hydrotreating is performed at temperatures in the range 280°C to 400°C, preferably 340°C to 380°C at pressures in the range 500 to 3000 psi, hydrogen treat gas rate in the range of 500 to 5000 SCF/bbl and a flow velocity in the range 0.1 to 5 LHSV, preferably 1 to 2 LHSV.
The hydrotreated waxy oil is stripped to remove ammonia and H2S
and then is subjected to the hydrodewaxing process of the present invention.
The catalyst employed in the hydrodewaxing of waxy feeds in accordance with the present invention is a unitized mixed powdered pellet catalyst. The term "unitized" as used here and in the claims means that each pellet is one made by mixing together a powdered first catalytic component with a powdered second catalytic component and pelletizing the mixture to produce pellets each of which contain all of the powder components previously recited.
The unitized catalyst can be prepared by starting with individual f nished catalysts, pulverizing and powdering such individual finished catalysts, mixing the powdered materials together to form a homogeneous mass, then compressing/extruding and pelleting thus producing the unitized pellet catalysts comprising a mixture of the individual, different, and distinct catalyst components. Pulverizing and powdering is to a consistency achievable using a mortar and pestle or other such conventional powdering means.
The catalyst used in the process of the present invention comprises a metal hydrogenation component on a two component support. The metal hydrogenation component is at least one of a Group VIB or Group VIII metal, preferably a Group VIII metal, and more preferably Pt or Pd. The metal is dispersed on at least one of the first and second components of the support, and preferably on both components. Typically the metal will be present in an amount ranging from about 0.1 to about 30 wt%, and preferably about 0.1 to IO wt%. If the metal is a Group VIII noble metal, then the preferred amount is 0.1 to 5 wt%. The catalyst may also include a substantially inert binder or matrix material.
The first component is a catalytic dewaxing component including crystalline 10 and 12 ring molecular sieves. Crystalline molecular sieves include metallo-, e.g., alumino silicates, alumino phosphates and silicoalumino-phosphates. Examples of crystalline alumino silicates include zeolites, e.g., ZSM-5, ZSM-11, ZSM-12, Theta-1 (ZSM-22), ZSM-23, ZSM-35, ZSM-48 natural and synthetic ferrierites, ZSM-57, Beta Mordenite and Offretite.
Examples of crystalline alumino and silicoalumino-phosphates include SAPO-11, SAPO-41, SAPO-31, MAPO-11 and MAPO-31. Preferred include ZSM-5, ZSM-22, ZSM-23, ferrierites, and SAPO-11.
The second isomerization component can be any of the typical isomerization catalyst such as those comprising amorphous refractory metal oxide support base (e.g., alumina, silica alumina, zirconia, titania, etc.) on which has been preferably deposited a catalytically active metal selected from Group VI B, Group VII B, Group VIII metals and mixtures thereof, preferably Group VIII, more preferably noble Group VIII, most preferably Pt or Pd and optionally including a promoter or dopant such as halogen, phosphorus, boric, yttria, rare earth oxides, from e.g., La, Ce, etc., magnesia, etc. preferably halogen, yttria or magnesia, most preferably fluorine. The catalytically active metals are present in the range 0.1 to 5 wt%, preferably 0.1 to 3 wt%, more preferably 0.1 to 2 wt%, most preferably 0.1 to 1 wt%. The promoters and dopants are used to control the acidity of the isomerization catalyst. Thus, when the isomerization catalyst employs a base-material such as alumina, acidity is imparted to the resultant catalyst by addition of a halogen, preferably fluorine. When a halogen is used, preferably fluorine, it is present in an amount in the range 0.1 to 10 wt%, prefer-ably 0.1 to 3 wt%, more preferably 0.1 to 2 wt%, most preferably 0.5 to 1.5 wt%. Similarly, if silica-alumina is used as the base material, acidity can be controlled by adjusting the ratio of silica to alumina or by adding a dopant such as yttria, rare earth oxides, from, e.g., La, Ce, etc., boric or magnesia which reduces the acidity of the silica-alumina base material as taught on U.S.
Patent 5,254,518 (Soled, McVicker, Gates, Miseo).
The first and second components are combined in a ratio sufficient to promote wax isomerization and napthene destruction without substantial decrease in VI. The zeolite to amorphous inorganic oxide ratios for catalysts according to the invention range from about 1:1 to 1:20 by weight, subject to the MC~I test described below.
One technique for determining the proper ratio of first and second components in the catalyst is based on an evaluation of the combined components containing about 0.5 wt% Pt in converting methylcyclohexane (MCP to various cyclopentane compounds. Catalyst that at 320°C provide a ratio of traps-1,2-dimethylcyclopentane to traps-1,3-dimethylcyclopentane (traps-l,2/trans-1,3 DMCP) in the range of at least one have been found to promote wax isomerization and naphathene destruction of feeds without substantial decrease in VI.
The second factor is when the catalyst, impregnated with about 0.5 wt% Pt and evaluated in converting methylcyclohexane (MCH) to various cyclopentane compounds at 10% conversion, exhibits a selectivity for ethyl-cyclopentane (ECP) formation above at least 50%.
This technique is fiuther explained as follows. The reaction of MCH over the catalyst to various cyclopentane products is shown in Figure 1.
As indicated in Figure 1, the products of MCH decomposition include ethyl-cyclopentane, cis- and traps-1,2-dimethylcyclopentane, cis- and traps-1,3-dimethylcyclopentane and 1,1 dimethylcyclopentane. This technique, also known as the MCH test is used to define relative acid site concentration, strengths and active site constraint for the catalysts according to the invention.
The key factors are summarized as follows: (1) total conversion of MCH for a given catalyst weight at 320°C is an indication of the relative number of acid sites; (2) selectivity to ECP, at 10% conversion, is a measure of the relative acid strength wherein high ECP selectivity values indicates low acid strength and low ECP selectivity values indicates high acid strength; and (3) the ratio of traps-1,2-DCMP to traps-1,3-DCMP correlates with the constraint at the catalyst active site wherein a high ratio (> 1 ) indicates little or no physical constraint at the active site and a low ratio (<1) indicates a physical constraint at the active site.
In the present process, to produce a catalyst that will give improved low temperature properties, the ratio of traps-1,2-DCMP to traps-1,3-DCMP is adjusted to from 1:1 to 2:1 predominately by controlling the acid _g_ strength of the amorphous isomerization component. It is preferred to use higher acid strength amorphous components such as silica-alumina.
Conversely, a catalyst that will give high yield is produced by decreasing the acid strength of the amorphous phase. In this case it is preferred to use lower acid strength amorphous components such as alumina. Another way of making such a catalyst is by changing the ratio of the microporous component to the amorphous component such that the unitized catalyst has a traps-1,2 traps-1,3 DMCP ratio of less than 1.
The hydrodewaxing process utilizing the catalyst of the present invention is conducted at temperatures between about 200°C to 400°C, prefer-ably 250°C to 380°C and most preferably 300°C to 350°C at pressures between about 500 to 5,000 psig (3.55 to 34.6 mPa), preferably 1,000 to 2000 psig (7.0 to 13.9 mPa), a hydrogen gas treat ratio of 500 to 10000 SCF H2B (89 to 1780 m3/m3), preferably 2,000 to 5,000 SCF HZB (356 to 890 m3/m3) and a LHSV
of 0.5 to 5 v/v/hr, preferably 1 to 2 v/v/hr.
In an alternate embodiment of the present invention the feed is first subject to solvent dewaxing to a pour point on the order of +10°C or lower.
The dewaxing solvent used may include the C3-C6 ketones such as methyl ethyl ketone (MEK), methyl isobutyl ketone (NIIBK), mixtures of MEK
and MIBK, aromatic hydrocarbons like toluene, mixtures of ketones and aromatics like MEK/toluene, ethers such as methyl t-butyl ethers and mixtures of same with ketones or aromatics. Similarly, liquefied, normally gaseous hydro-carbons like propane, propylene, butane, butylene, and combinations thereof may be used as the solvent. Preferably the solvent employed will be an equal _g_ volume mixture of methyl ethyl ketone and methyl isobutyl ketone. Typically the isomerate to solvent ratio will range between 1 to 10 and preferably will be about 1:3. The dewaxed feed is then subjected to hydrodewaxing as described hereinabove.
The present invention is demonstrated below in the non-limiting examples.
EXAMPLES
Comparative Example 1 A catalyst (B) comprising 0.5 wt% Pt ZSM-5 (silica/alumina ratio 220:1) and alumina in the weight ratio of 25:75, was used in two runs to dewax a hydrocrackate distillate having the following properties:
KV, cSt at 100°C 3.808 KV, cSt at 135°C 2.28 Pour Point, °C 39 Boiling Range (GCD) 325-503°C
The dewaxing conditions employed are listed in the accompanying Table. The results are shown in column B of the Table following Example 2.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 40 and a trans-1, 2/trans-1,3 dimethylcylopentane ratio of 0.02 as shown in the Table. A comparison of columns A and B of the Table shows that the VI of the resulting liquid product (350°C+) was lower than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brool~eld Viscosity at -40°C
(additized with a standard Ford type ATF adpack), are also shown in the Table. The Brookfield Viscosity is reduced by catalytic dewaxing over that of a solvent dewaxed product. However, the Brookfield Viscosities of both solvent and cat dewaxed products are very poor.
Comparative Example 2 A catalyst (C) comprising 0.5 wt% Pt ZSM-5 (silicalalumina ratio 220:1) and silica-alumina in the weight ratio of 50:50, was used to dewax a hydrocrackate distillate having the properties noted in Comparative Example 1.
This catalyst was made by combining the powdered ZSM-S (Si/Al ratio 110) with the powdered amorphous component in the weight ratio of 50:50 and then loading platinum by incipient wetness using platinum tetraamine dichloride.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 47 and a traps-1, 2/trans-1,3 dimethylcylopentane ratio of 0.82 as shown in the Table following Example 2.
A comparison of columns A and C, in the Table shows that the VI of the resulting liquid product (350°C+) was lower than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brool~ield Viscosity -40°C (additized with a standard Ford type ATF adpack), are also shown in the Table. The Brookfield Viscosity is reduced by catalytic dewaxing over that of a solvent dewaxed product but not significantly over that obtained using the alumina bound catalyst in Example 1.
Example 1 A catalyst (D) comprising 0.5 wt% Pt ZSM-5 (silica/alumina ratio 220:1) and silica alumina in the weight ratio of 10:90, was used to dewax a hydrocrackate distillate having the properties noted in Comparative Example 1.
This catalyst was made by combining the powdered ZSM-5 (Si/Al ratio 110) with the powdered amorphous component in the weight ratio of 10:90 respectively and then loading platinum by incipient wetness using platinum tetraamine dichloride.
When screened for activity and selectivity with methylcyclo-hexane, this catalyst had an ECP selectivity of 50 and a traps-1,2/trans-1,3 dimethylcylopentane ratio of 1.80 as shown in the Table following Example 2.
Both of these values are within the criteria for catalysts of this invention.
A
comparison of columns A and D, in Table 1 shows that the VI of the resulting liquid product (350°C+) w~ lugher than that obtained by solvent dewaxing. The product low temperature properties, as shown by the Brookfield Viscosity at -40°C (addized in a standard ECA/ATF adpack), are also shown in the Table.
The Brookfield Viscosity is significantly reduced by catalytic dewaxing with this catalyst over that of a solvent dewaxed product in the Table 1.
Example 2 The procedure of Example 1 was followed using 0.5 wt% on Pt on theta-1 (TON) on silica-alutnina (Catalyst E)and 0.5 wt% Pt on A1203 in the weight ratio of 25:75 (Catalyst F-Comparative). Theta-1 is a 10 ring zeolite and is described in EP 057049. This catalyst was made by combining the powdered TON zeolite (Si/Al ratio 30) with the powdered amorphous component in different ratios and then loading platinum by incipient wetness using platinum tetraamine dichloride. The condition and results are set out in columns E and F
of Table 1.
~
N 'n O ~ .-. ~ ~ ~ N
en ...~ .-. ~ ~ Oy l~ r., ...r ~ O ....
~'y M ." N M .-. ' ~ N C
~
N
v.r ~ tef M
p~ v1 ... N 'n x, .-~ v1 .-, N 00 .-.
w ~ ~ ~ ~ N ~ M ~~r ' ,~." ~ r";
H
'b ~
M ~ 00 M g v.r M ~ M l~ ~' M N
.-w .--~
A
N $ "", N 0M0~ M ~ N .-N, 10 00 M ~", N M ~ ,.., , N ...:
O
~-~ O ~ N O O 0~0 O M
M ~ ~. ~ .-' h U ~ a E
N ' O o0 " N M v0 N
.-' ~ ..w ~ h N ~ ~ 00 M ,~ N ~ ~ ~ ' pp "", C
~_ ~ h ~ O M
M h ~' N rr , N
N
N a ~ .~ g N o ~ o ~ g ~ O o ~a M ~ N ~~~,~ , ~ ~~o "'~~°°N ° ~~z d ~ M CO ~. , n U
° U U
o ~ °
..~. OV .~~~r' N M
w o U .a .~ ~ U o ..
o z ~ ~w ~ ~a~~ °
-~ V v Or~4 ~ ~ E..~~?~ ~~ ~ ~V o s ~pG+.~.~ ~° ~°vO, ~
0 0 ~ .~ .N o V ~~Hw >H ~~M»~a, ~p~., ~Uw~A
The results shown in the Table are further illustrated in Figure 2 which is a graph showing Brool~eld viscosity vs. yield for various catalyst combinations.
Claims (14)
1. A method for hydrodewaxing of feeds to produce a tube base-stock having improved low temperature properties which comprises:
contacting the feed with a unitized mixed powder pellet catalyst under hydrodewaxing conditions, the catalyst comprising a metal hydrogenation component on a support having a first dewaxing component and a second isomerization component, wherein the first component is selected from 10 and 12 ring molecular sieve and mixtures thereof and the second component is an amorphous inorganic oxide and wherein the first and second components are present in a ratio such that when evaluated in the conversion of methyl cyclohexane at 320°C to 1,1-dimethylcyclopentane, 1,2-dimethylcyclopentane, 1,3-dimethylcyclopentane and ethylcyclopentane, the catalyst will provide a trans-1,2-/traps-1,3-dimethylcyclopentane ratio is at least 1 and a selectivity to ethylcyclopentane, at 10% conversion, of at least about 50%.
contacting the feed with a unitized mixed powder pellet catalyst under hydrodewaxing conditions, the catalyst comprising a metal hydrogenation component on a support having a first dewaxing component and a second isomerization component, wherein the first component is selected from 10 and 12 ring molecular sieve and mixtures thereof and the second component is an amorphous inorganic oxide and wherein the first and second components are present in a ratio such that when evaluated in the conversion of methyl cyclohexane at 320°C to 1,1-dimethylcyclopentane, 1,2-dimethylcyclopentane, 1,3-dimethylcyclopentane and ethylcyclopentane, the catalyst will provide a trans-1,2-/traps-1,3-dimethylcyclopentane ratio is at least 1 and a selectivity to ethylcyclopentane, at 10% conversion, of at least about 50%.
2. The method of claim 1 wherein the metal hydrogenation component is at least one of a Group VI or Group VIII metal.
3. The method of claim 2 wherein the metal hydrogenation component is a Group VIII metal.
4. The method of claim 2 wherein the metal hydrogenation component is dispersed on at least one of the first and second components.
5. The method of claim 4 wherein the hydrogenation component is dispersed on both the first and second component.
6. The method of claim 4 or 5 wherein the hydrogenation component is dispersed in an amount ranging from about 0.1 wt% to about 30 wt%.
7. The method of claim 2 wherein in the second component when evaluated in the conversion of methylcyclohexane at 320°C will exhibit a selectivity for ECP formation of at least 50% or greater.
8. The process of claim 1 wherein the feed is a feed that is solvent dewaxed to a pour point of up to +10°C.
9. The process of claim 1 wherein the feed is hydrotreated at temperatures in the range 280°C to 400°C, at pressures in the range 500 to 3000 psi, hydrogen treat gas rate in the range of 500 to 5000 SCF/bb1 and a flow velocity in the range 0.1 to 5 LHSV.
10. The process of claim 1 wherein the 10 and 12 ring molecular sieves are selected from alumino silicates and alumino phosphates.
11. The process of claim 10 wherein the alumino silicates are selected from ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, natural and synthetic ferreirites, ZSM-57, Beta Mordenite and Offretite.
12. The process of claim 10 wherein the alumino phosphates are selected from SAPO-11, SAPO-41, SAPO-31, MAPO-11 and MAPO-31.
13. The process of claim 10 wherein the molecular sieves are selected from ZSM-5, ZSM-22, ZSM-23, ferrierites and SAPO-11.
14. The process of claim 1 wherein the amorphous inorganic oxide is promoted or doped with yttria, rare earth oxides, boria and magnesia.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US7472298P | 1998-02-13 | 1998-02-13 | |
| US60/074,722 | 1998-02-13 | ||
| PCT/US1999/003006 WO1999041334A1 (en) | 1998-02-13 | 1999-02-12 | Process for improving basestock low temperature performance using a combination catalyst system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2320106A1 true CA2320106A1 (en) | 1999-08-19 |
Family
ID=22121273
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002320106A Abandoned CA2320106A1 (en) | 1998-02-13 | 1999-02-12 | Process for improving basestock low temperature performance using a combination catalyst system |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP1054938A4 (en) |
| JP (1) | JP2002503754A (en) |
| AU (1) | AU743235B2 (en) |
| CA (1) | CA2320106A1 (en) |
| WO (1) | WO1999041334A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9045702B2 (en) | 2009-03-31 | 2015-06-02 | Jx Nippon Oil & Energy Corporation | Method for producing lubricant base oil |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2505607A1 (en) * | 2000-11-16 | 2004-05-27 | Exxonmobil Research And Engineering Company | Process for improving basestock low temperature performance using a combination catalyst system |
| US7208442B2 (en) | 2002-02-28 | 2007-04-24 | Exxonmobil Chemical Patents Inc. | Molecular sieve compositions, catalyst thereof, their making and use in conversion processes |
| US6906232B2 (en) | 2002-08-09 | 2005-06-14 | Exxonmobil Chemical Patents Inc. | Molecular sieve compositions, catalysts thereof, their making and use in conversion processes |
| US6995111B2 (en) | 2002-02-28 | 2006-02-07 | Exxonmobil Chemical Patents Inc. | Molecular sieve compositions, catalysts thereof, their making and use in conversion processes |
| US7319178B2 (en) | 2002-02-28 | 2008-01-15 | Exxonmobil Chemical Patents Inc. | Molecular sieve compositions, catalysts thereof, their making and use in conversion processes |
| ATE316562T1 (en) | 2002-07-12 | 2006-02-15 | Shell Int Research | METHOD FOR PRODUCING A HEAVY AND A LIGHT LUBRICANT L-GROUND LS |
| US7867957B2 (en) | 2007-03-30 | 2011-01-11 | Nippon Oil Corporation | Lubricating oil composition |
| EP2135928B1 (en) | 2007-03-30 | 2013-08-21 | Nippon Oil Corporation | Lubricant base oil, method for production thereof, and lubricant oil composition |
| CN103923726A (en) | 2007-12-05 | 2014-07-16 | 吉坤日矿日石能源株式会社 | Lubricant Oil Composition |
| JP5483662B2 (en) | 2008-01-15 | 2014-05-07 | Ｊｘ日鉱日石エネルギー株式会社 | Lubricating oil composition |
| JP5806794B2 (en) | 2008-03-25 | 2015-11-10 | Ｊｘ日鉱日石エネルギー株式会社 | Lubricating oil composition for internal combustion engines |
| US8648021B2 (en) | 2008-10-07 | 2014-02-11 | Jx Nippon Oil & Energy Corporation | Lubricant base oil and a process for producing the same, and lubricating oil composition |
| JP2010090251A (en) | 2008-10-07 | 2010-04-22 | Nippon Oil Corp | Lubricant base oil, method for producing the same, and lubricating oil composition |
| EP2497820B1 (en) | 2008-10-07 | 2016-06-29 | JX Nippon Oil & Energy Corporation | Lubricant composition |
| CN102459543A (en) | 2009-06-04 | 2012-05-16 | 吉坤日矿日石能源株式会社 | A lubricating oil composition and a method for making the same |
| EP2439259A4 (en) | 2009-06-04 | 2014-03-12 | Jx Nippon Oil & Energy Corp | Lubricant oil composition |
| EP2573155B1 (en) | 2009-06-04 | 2016-07-13 | JX Nippon Oil & Energy Corporation | Lubricating oil composition |
| JP5689592B2 (en) | 2009-09-01 | 2015-03-25 | Ｊｘ日鉱日石エネルギー株式会社 | Lubricating oil composition |
| US20150060327A1 (en) | 2012-03-30 | 2015-03-05 | Jx Nippon Oil & Energy Corporation | Lubricant base oil and method for producing same |
| WO2013147302A1 (en) | 2012-03-30 | 2013-10-03 | Ｊｘ日鉱日石エネルギー株式会社 | Lubricant base oil and method for producing same |
Family Cites Families (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3755145A (en) * | 1971-03-17 | 1973-08-28 | Mobil Oil Corp | Lube oil hydrocracking with zsm-5 zeolite |
| US4181598A (en) * | 1977-07-20 | 1980-01-01 | Mobil Oil Corporation | Manufacture of lube base stock oil |
| US4437975A (en) * | 1977-07-20 | 1984-03-20 | Mobil Oil Corporation | Manufacture of lube base stock oil |
| US4259170A (en) * | 1979-09-14 | 1981-03-31 | Mobil Oil Corporation | Process for manufacturing lube base stocks |
| US4428862A (en) * | 1980-07-28 | 1984-01-31 | Union Oil Company Of California | Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons |
| US4600497A (en) * | 1981-05-08 | 1986-07-15 | Union Oil Company Of California | Process for treating waxy shale oils |
| US4510044A (en) * | 1982-02-08 | 1985-04-09 | Mobil Oil Corporation | Process for hydrotreating petroleum residua and catalyst therefor |
| US4414097A (en) * | 1982-04-19 | 1983-11-08 | Mobil Oil Corporation | Catalytic process for manufacture of low pour lubricating oils |
| US4960504A (en) * | 1984-12-18 | 1990-10-02 | Uop | Dewaxing catalysts and processes employing silicoaluminophosphate molecular sieves |
| US4867861A (en) * | 1985-06-18 | 1989-09-19 | Union Oil Company Of California | Process and catalyst for the dewaxing of shale oil |
| US4859311A (en) * | 1985-06-28 | 1989-08-22 | Chevron Research Company | Catalytic dewaxing process using a silicoaluminophosphate molecular sieve |
| US5246566A (en) * | 1989-02-17 | 1993-09-21 | Chevron Research And Technology Company | Wax isomerization using catalyst of specific pore geometry |
| US5082986A (en) * | 1989-02-17 | 1992-01-21 | Chevron Research Company | Process for producing lube oil from olefins by isomerization over a silicoaluminophosphate catalyst |
| DK0458895T3 (en) * | 1989-02-17 | 1995-11-06 | Chevron Usa Inc | Isomerization of waxy lubricating oils and petroleum wax using a silicoaluminophosphate molsi catalyst |
| US5139647A (en) * | 1989-08-14 | 1992-08-18 | Chevron Research And Technology Company | Process for preparing low pour middle distillates and lube oil using a catalyst containing a silicoaluminophosphate molecular sieve |
| US5332490A (en) * | 1992-09-28 | 1994-07-26 | Texaco Inc. | Catalytic process for dewaxing hydrocarbon feedstocks |
| US5885438A (en) * | 1993-02-12 | 1999-03-23 | Mobil Oil Corporation | Wax hydroisomerization process |
| DE69525469T2 (en) * | 1994-11-22 | 2002-06-27 | Exxonmobil Res & Eng Co | METHOD FOR IMPROVING WAXY INSERT BY A CATALYST COMPOSED AS A MIXTURE OF A PULVERIZED DEWaxING CATALYST AND A PULVERIZED ISOMERIZATION CATALYST, SHAPED AS A PARTICULATE PART |
-
1999
- 1999-02-12 EP EP99906941A patent/EP1054938A4/en not_active Withdrawn
- 1999-02-12 JP JP2000531518A patent/JP2002503754A/en active Pending
- 1999-02-12 CA CA002320106A patent/CA2320106A1/en not_active Abandoned
- 1999-02-12 AU AU26734/99A patent/AU743235B2/en not_active Ceased
- 1999-02-12 WO PCT/US1999/003006 patent/WO1999041334A1/en not_active Application Discontinuation
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9045702B2 (en) | 2009-03-31 | 2015-06-02 | Jx Nippon Oil & Energy Corporation | Method for producing lubricant base oil |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2002503754A (en) | 2002-02-05 |
| EP1054938A4 (en) | 2004-12-01 |
| AU2673499A (en) | 1999-08-30 |
| AU743235B2 (en) | 2002-01-24 |
| WO1999041334A1 (en) | 1999-08-19 |
| EP1054938A1 (en) | 2000-11-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU743235B2 (en) | Process for improving basestock low temperature performance using a combination catalyst system | |
| US5723716A (en) | Method for upgrading waxy feeds using a catalyst comprising mixed powdered dewaxing catalyst and powdered isomerization catalyst formed into a discrete particle (LAW082) | |
| EP1244762B1 (en) | A diesel fuel having a very high iso-paraffin to normal paraffin mole ratio | |
| US6620312B1 (en) | Process for making a lube basestock with excellent low temperature properties | |
| US5977425A (en) | Method for upgrading waxy feeds using a catalyst comprising mixed powdered dewaxing catalyst and powdered isomerization catalyst formed into a discrete particle | |
| EP0938532A1 (en) | Process for highly shape selective dewaxing which retards catalyst aging | |
| JPH10503542A (en) | Production of lubricating oils with VI-selective catalysts | |
| JP2002503756A (en) | Lubricating oil production with mixed catalyst systems. | |
| AU742605B2 (en) | Process for making a lube basestock | |
| EP1562703A1 (en) | Process for improving basestock low temperature performance using a combination catalyst system | |
| US20060142142A1 (en) | Process for improving basestock low temeperature performance using a combination catalyst system | |
| US20060138023A1 (en) | Process for making a lube basestock |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |