EP1562703A1 - Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine - Google Patents

Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine

Info

Publication number
EP1562703A1
EP1562703A1 EP02789641A EP02789641A EP1562703A1 EP 1562703 A1 EP1562703 A1 EP 1562703A1 EP 02789641 A EP02789641 A EP 02789641A EP 02789641 A EP02789641 A EP 02789641A EP 1562703 A1 EP1562703 A1 EP 1562703A1
Authority
EP
European Patent Office
Prior art keywords
zsm
component
catalyst
mixtures
dimethylcyclopentane
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.)
Withdrawn
Application number
EP02789641A
Other languages
German (de)
English (en)
Inventor
William J. Murphy
Ian A. Cody
Robert J. Wittenbrink
Stuart L. Soled
Gary B. Mcvicker
Sylvain S. Hantzer
Sandra J. Linek
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Research and Engineering Co
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by ExxonMobil Research and Engineering Co filed Critical ExxonMobil Research and Engineering Co
Publication of EP1562703A1 publication Critical patent/EP1562703A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/74—Noble metals
    • B01J29/7484—TON-type, e.g. Theta-1, ISI-1, KZ-2, NU-10 or ZSM-22
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12—Silica and alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/064—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing iron group metals, noble metals or copper
    • B01J29/068—Noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/44—Noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/19—Catalysts containing parts with different compositions
    • 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
    • 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
    • C10G45/62—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 platinum group metals or compounds thereof
    • 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

Definitions

  • This invention relates to the hydrodewaxing of waxy feeds including slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate, waxy raffinates, and waxy distillates to produce a lube 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 lube basestock with minimum VI loss and having good 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 paraffins typically results in a loss of viscosity index (VI) which is undesirable.
  • VI viscosity index
  • United States Patent Number 4,428, 865, Oleck, et al. claims a method to enhance the pour point and viscosity index of crude oils of high wax content by contacting the highly waxy feed with two different zeolites such as ZSM-5 and ZSM-35.
  • isomerization of waxy feeds using molecular sieve based catalyst that have linear ID pore structures produces lube 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 lube basestocks without significant loss in VI and which basestock has good low temperature properties.
  • This invention relates to a method for the hydrodewaxing of feeds to produce a lube basestock having improved low temperature properties which comprises:
  • a unitized mixed powder pellet catalyst under hydrodewaxing conditions, said catalyst comprising: (i) a first dewaxing component selected from 10 and 12 ring molecular sieves and mixtures thereof having a metal hydrogenation component dispersed thereon; (ii) a second component selected from amorphous inorganic oxides said second component having a metal hydrogenation component dispersed thereon; and (iii) wherein said 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- /trans- 1,3-dimethylcyclopentane ratio in the range of about 1:1 to about 1:2 and a selectivity to ethylcyclopentane, at 10% conversion, of at least about 50%
  • 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.
  • 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 raffinates and waxy distillates. Typically, such feeds will have wax contents of 15% or more.
  • the preferred feed will have a nitrogen and sulfur 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 conditions 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.
  • any of the Group VIB to Group VIII metals and mixtures thereof are those metals of the Periodic Table of Elements; Sargent- Welch Scientific Co.) on metal oxide refractory supports may be employed.
  • Non-limiting commercial examples of such are identified as HDN-30, KF-840, KF-848, etc.
  • 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 10 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 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, Co/Ni/Mo on alumina, e.g., KF-840, KF-843, HDN-30, HDN-60, Criteria C-411, etc.
  • 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.
  • 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 finished 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, Pd, and mixtures thereof.
  • the metal is dispersed 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 10 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 alumino silicates and alumino phosphates.
  • Examples of crystalline alumino silicates include zeolites such as ZSM-5, ZSM-11, ZSM-12, Theta-1 (ZSM-22), ZSM-23, ZSM-35, natural and synthetic ferrierites, ZSM-48, ZSM-57, SSZ-31, Beta, Mordenite, Offretite, ECR-42, MCM-71, and ITQ-13.
  • Examples of crystalline alumino phosphates include SAPO-11, SAPO-41, SAPO-31, MAPO- 11 and MAPO-31.
  • Preferred molecular sieves include ZSM-5, ZSM-22, ZSM- 23, ZSM-48, ferrierites, SSZ-31, SAPO-11, ECR-42, MCM-71, and ITQ-13.
  • the most preferred molecular sieves are ZSM-48, ECR-42, MCM-71, SSZ-31, and ITQ-13.
  • 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 at least one Group VIII, more preferably at least one noble Group VIII, most preferably Pt, Pd, and mixtures thereof, and optionally including a promoter or dopant such as halogen, phosphorus, boria, yttria, rare earth oxides, from e.g., La, Ce, etc., magnesia, etc.
  • amorphous refractory metal oxide support base e.g., alumina, silica-alumina, zirconia, titania, etc.
  • a catalytically active metal selected from Group VI B, Group VII B, Group VIII
  • 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.%o, most preferably 0.1 to 1 wt.%.
  • the promoters and dopants are used to control the acidity of the isomerization catalyst.
  • acidity is imparted to the resultant catalyst by addition of a halogen, preferably fluorine.
  • a halogen preferably fluorine
  • it is present in an amount in the range 0.1 to 10 wt.%, preferably 0.1 to 3 wt.%, more preferably 0.1 to 2 wt.%), most preferably 0.5 to 1.5 wt.%.
  • 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., boria or magnesia which modifies the acidity of the silica-alumina base material as taught on U.S. Patent 5,254,518 (Soled, McVicker, Gates, Miseo).
  • both the first and second components be at least one crystalline 10 or 12 ring molecular sieve.
  • the first and second components can also be selected from mixtures of 10 and 12 ring molecular sieves.
  • both the first and second components can be selected from any of the 10 and 12 ring molecular sieves listed above, and mixtures thereof.
  • the first component be ITQ-13 and the second component be selected from ZSM-48, ZSM-35, ZSM-22, ZSM-23, ZSM-57, SSZ-31, and mixtures thereof.
  • the first component be selected from ITQ-13, ZSM-57, and mixtures thereof
  • the second component be selected from ZSM-22, ZSM-23, ZSM-35, ZSM-48, SSZ-31, and mixtures thereof.
  • 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 MCH 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 (MCH) to various cyclopentane compounds.
  • Catalyst that at 320°C provide a ratio of trans 1,2-dimethylcyclopentane to trans 1,3-dimethylcyclopentane (trans- 1,2/trans- 1,3 DMCP) in the range of greater than one, e.g., 1:1 to 2:1 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 ethylcyclopentane (ECP) formation above at least 50%>.
  • MCH methylcyclohexane
  • ECP ethylcyclopentane
  • the ratio of trans- 1,2-DCMP to trans-l,3-DCMP is adjusted to from 1:1 to 2:1 predominately by controlling the acid strength of the amorphous isomerization component. It is preferred to use higher acid strength amorphous components such as silica-alumina.
  • a catalyst that will give high yield is produced by decreasing the acid strength of the amorphous phase.
  • 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 trans- 1,2 trans- 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, preferably 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 H 2 /B (89 to 1780 m 3 /m 3 ), preferably 2,000 to 5,000 SCF H 2 /B (356 to 890 m3/ m 3) and a LHSV of 0.5 to 5 v/v/hr, preferably 1 to 2 v/v/hr.
  • the feed is first subjected to solvent dewaxing to a pour point on the order of +10°C or lower.
  • the dewaxing solvent used may include the C3- 5 ketones such as methyl ethyl ketone (MEK), methyl isobutyl ketone (MIBK), 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.
  • MEK methyl ethyl ketone
  • MIBK methyl isobutyl ketone
  • aromatic hydrocarbons like toluene
  • ethers such as methyl t-butyl ethers and mixtures of same with ketones or aromatics.
  • liquefied, normally gaseous hydrocarbons like propane, propylene, butane, butylene, and combinations thereof may be used as the solvent.
  • the solvent employed will be an equal volume mixture of methyl ethyl ketone and methyl isobutyl ketone.
  • the isomerate to solvent ratio will range between 1 to 10 and preferably will be about 1:3.
  • 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:
  • a catalyst (C) comprising 0.5 wt.% Pt ZSM-5 (silica/alumina 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-5 (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.
  • this catalyst When screened for activity and selectivity with methylcyclohexane, this catalyst had an ECP selectivity of 47 and a t-1, 2/t-l,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 Brookfield 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.
  • 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.
  • this catalyst When screened for activity and selectivity with methylcyclohexane, this catalyst had an ECP selectivity of 50 and a t-l,2/t-l,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 the Table shows that the VI of the resulting liquid product (350°C+) was higher 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 of the Table.
  • Example 1 The procedure of Example 1 was followed using 0.5 wt.%> on Pt on theta-1 (TON) on silica-alumina (Catalyst E) and 0.5 wt.%> Pd on AI2O3 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 the Table.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Lubricants (AREA)

Abstract

Selon l'invention, des charges paraffineuses sont transformées en une huile de base au moyen d'un catalyseur sous forme de pastilles de poudre mixtes unitaires comprenant un composant d'hydrogénation métallique sur un support comportant un premier composant de déparaffinage et un second composant d'isomérisation, le premier composant étant choisi parmi des tamis moléculaires à 10 et 12 cycles et des mélanges de ceux-ci et le second composant étant un oxyde inorganique amorphe. Le premier et le second composant sont présents selon un rapport suffisant pour favoriser l'isomérisation de la paraffine et la destruction du naphtène sans réduction sensible de l'indice de viscosité.
EP02789641A 2000-11-16 2002-11-12 Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine Withdrawn EP1562703A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US60155200A 2000-11-16 2000-11-16
PCT/US2002/036522 WO2004043594A1 (fr) 2000-11-16 2002-11-12 Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine

Publications (1)

Publication Number Publication Date
EP1562703A1 true EP1562703A1 (fr) 2005-08-17

Family

ID=32313255

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02789641A Withdrawn EP1562703A1 (fr) 2000-11-16 2002-11-12 Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine

Country Status (5)

Country Link
EP (1) EP1562703A1 (fr)
JP (1) JP2006509847A (fr)
AU (1) AU2002352693A1 (fr)
CA (1) CA2505607A1 (fr)
WO (1) WO2004043594A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105582985B (zh) * 2014-10-22 2018-01-16 中国石油化工股份有限公司大连石油化工研究院 一种石蜡烃择型异构化催化剂的原位预处理方法
CN105582987B (zh) * 2014-10-22 2018-01-16 中国石油化工股份有限公司大连石油化工研究院 一种石蜡烃择型异构化催化剂的预处理方法
CN114471692B (zh) * 2020-11-12 2024-04-30 中国石油天然气股份有限公司 一种加氢异构催化剂及其载体的制备方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4575416A (en) * 1984-07-16 1986-03-11 Mobil Oil Corporation Hydrodewaxing with mixed zeolite catalysts
EP0183419A3 (fr) * 1984-11-28 1987-04-15 Mobil Oil Corporation Procédé de déparaffinage de distillat
US5977425A (en) * 1994-11-22 1999-11-02 Exxon Research And Engineering Co Method for upgrading waxy feeds using a catalyst comprising mixed powdered dewaxing catalyst and powdered isomerization catalyst formed into a discrete particle
WO1998002503A1 (fr) * 1996-07-15 1998-01-22 Chevron U.S.A. Inc. Systeme catalyseur a plusieurs couches pour hydroconversion d'huile lubrifiante
CA2320106A1 (fr) * 1998-02-13 1999-08-19 Exxon Research And Engineering Company Procede d'amelioration des performances d'une matiere de base, a basse temperature, a l'aide d'un systeme catalyseur combine
JP2002503753A (ja) * 1998-02-13 2002-02-05 エクソンモービル リサーチ アンド エンジニアリング カンパニー 潤滑用基材油の製造方法
US6652735B2 (en) * 2001-04-26 2003-11-25 Exxonmobil Research And Engineering Company Process for isomerization dewaxing of hydrocarbon streams

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2004043594A1 *

Also Published As

Publication number Publication date
CA2505607A1 (fr) 2004-05-27
WO2004043594A1 (fr) 2004-05-27
AU2002352693A1 (en) 2004-06-03
JP2006509847A (ja) 2006-03-23

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)
EP1062305B1 (fr) Huile de base a faible viscosite pour lubrifiants
US6620312B1 (en) Process for making a lube basestock with excellent low temperature properties
US5951848A (en) Process for highly shape selective dewaxing which retards catalyst aging
US5977425A (en) Method for upgrading waxy feeds using a catalyst comprising mixed powdered dewaxing catalyst and powdered isomerization catalyst formed into a discrete particle
EP0710710A2 (fr) Combinaison de catalyseurs pour isomérisation de cires
JPH10503542A (ja) Ｖｉ−選択性触媒による潤滑油の製造
JP2002503756A (ja) 混合触媒系による潤滑油の製造
AU742605B2 (en) Process for making a lube basestock
EP1562703A1 (fr) Procede d'amelioration des performances a basse temperature d'une huile de base au moyen d'un systeme catalyseur combine
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
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20050531

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK RO SI

DAX Request for extension of the european patent (deleted)
RIN1 Information on inventor provided before grant (corrected)

Inventor name: LINEK, SANDRA, J.

Inventor name: HANTZER, SYLVAIN, S.

Inventor name: MCVICKER, GARY, B.

Inventor name: SOLED, STUART, L.

Inventor name: WITTENBRINK, ROBERT, J.

Inventor name: CODY, IAN, A.

Inventor name: MURPHY, WILLIAM, J.

17Q First examination report despatched

Effective date: 20081229

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20090509