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
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group 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
  • B01J29/064—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
  • 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
  • B01J29/80—Mixtures of different zeolites
• • 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
  • 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
• • 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
  • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
  • B01J35/391—Physical properties of the active metal ingredient
  • B01J35/394—Metal dispersion value, e.g. percentage or fraction
• • 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

Definitions

• This invention relates to the hydroisomerization of waxy feeds including slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch hydroisomerate waxy raffmates, 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 having a preselected acidity capable of promoting the formation of a basestock having a predetermined (VI) within a range of Vis.
• a mixed catalyst having a preselected acidity capable of promoting the formation of a basestock having a predetermined (VI) within a range of Vis.
• 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 (VI) which is undesirable.
• VI viscosity
• United States Patent Number 4,428, 865, Oleck, et al. claims a method to enhace the pour point and visosity 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.
• the presently disclosed invention is a method for hydroisomerizing a waxy feed to produce improved yield of a lube basestock which comprises:
• a first dewaxing component selected from 8, 10 and 12 ring molecular sieves and mixtures thereof having a metal hydrogenation component dispersed thereon;
• both the first and second component comprise at least one 8, 10 ior 12 ring molecular sieve or a mixture thereof. Both the first and second component have a metal hydrogenation component dispersed thereon.
• Figure 1 is a schematic drawing showing the conversion of methylcyclohexane to various cyclopentane compounds at 320°C.
• 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 isomerate waxy raffmates and waxy distillates.
• waxy hydrocarbon oils such as slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch isomerate waxy raffmates and waxy distillates.
• waxy hydrocarbon oils such as slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch isomerate waxy raffmates and waxy distillates.
• waxy hydrocarbon oils such as slack wax, slack wax isomerate, Fischer-Tropsch wax, Fischer-Tropsch isomerate waxy raffmates and waxy distillates.
• Such feeds will have wax contents of 15% or more.
• the preferred feed will have a nitrogen and sulfur content each below about 20% or more.
• the preferred feed will have
• any of the conventional hydrotreating 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. are those metals of the Periodic Table of Elements; Sargent- Welch Scientific Co.
• Non-limiting commercial examples of such are identified as HDN- 30, KF-840, and KF-848, etc.
• Hydrotreating is conducted so as to lower the sulfur and nitrogen contents to levels of 20 wppm or less nitrogen or 20 wppm 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 hydroisomerization process of the present invention.
• the catalyst employed in the hydroisomerization 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 component with a powdered second 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 powdered components pulverizing and powdering such individual finished components, mixing the powdered materials together to form a homogeneous mass, then compressing/extruding and pelleting thus producing the unitized pellet catalysts. Pulverizing and powdering is to a consistency achievable using a ball mill or other such conventional powdering means to a particle size less than 100 microns.
• the first component is a catalytic dewaxing component including crystalline 8, 10 and 12 ring molecular sieves.
• Crystalline molecular sieves include alumino silicates and alumino phosphates.
• Examples of crystalline alumino silicates include zeolites such as erionite, chabazite, 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 aluminum 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, zirconia, titania, silica-magnesia, silica-alumina, 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 lease one Group VIII metal, more preferably at least one noble Group VIII metal, most preferably Pt, Pd, and mixtures thereof, and optionally including a promoter or dopant such as halogen, phosphorus, boron, yttria, magnesia, etc., preferably halogen, yttria or magnesia, most preferably fluorine.
• amorphous refractory metal oxide support base e.g., alumina, silica, zirconia, titania, silica-magnesi
• 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.
• acidity of the resultant catalyst is reduced by addition of a basic material such as yttria or magnesia or by controlling the ratio of silica: aluminum in the silica-alumina.
• the metal hydrogenation component can be deposited on either the first dewaxing component, the second isomerization component or preferably on both the first and second components.
• the metal is selected from at least one of Group VIB and Group VIII, preferably Group VIII, more preferably Pt, Pd and mixtures thereof.
• the amount of metal can range from 0.1 to 30 wt%, based on catalyst. If the metal is Pt or Pd, the preferred amount is from 0.1 to 5 wt%, based on catalyst. In order to maximize catalyst utilization, it is preferred that the metal dispersion be at least 0.3 (on a scale where 100% metal dispersion is 1.0) if the metal is only on one component. If the metal is on both components, then it is preferred that the metal dispersion (D) times the metal concentration (C) (i.e., D x C) on one of the components be at least 0.08.
• the first and second components are combined in a ratio sufficient to promote wax isomerization and naphthene 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.
• the second factor is when the catalyst, impregnated with about 0.5 wt% Pt and evaluated in converting methylcyclohexane to various cyclopentane compounds at 10% conversion, exhibits a selectivity for ethylcyclopentane (ECP) formation above at least 50%.
• ECP ethylcyclopentane
• the ratio of trans- 1,2-DCMP to trans-l,3-DCMP is adjusted to less than about 1 predominantly by controlling both the number and strength of the amorphous isomerization component. It is preferred to use lower acid strength amorphous components such as alumina.
• a catalyst that will maximize VI is produced by increasing the acid strength of the amorphous phase.
• it is preferred to use higher acid strength amophous components such as silica-aluminas or modified silica-aluminas.
• 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- l,2/trans-l,3 DMCP ratio of >1.
• the hydroisomerization 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 hydrogen partial pressures between about 350 to 5,000 psig (2.41 to 34.6 mPa), preferably 1,000 to 2500 psig (7.0 to 17.2 mPa), a hydrogen gas treat ratio of 500 to 10,000 SCF H 2 /bbl (89 to 1780 m3/ m 3), preferably 2,000 to 5,000 SCF H 2 bbl (356 to 890 m3/m ) and a LHSV of 0.1 to 10 v/v/l ⁇ r, preferably 0.5 to 5 v/v/hr, and more preferably 1 to 2 v/v/hr.
• the waxy feed is first subject to solvent dewaxing to a pour point of 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 (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.
• both the first and second components be at least one crystalline 8, 10 or 12 ring molecular sieves. It is also contemplated that both the first and second components be a mixture of 8, 10 or 10 ring molecular sieves. Thus, both the first and second components can be selected from any of the 8, 10 and 12 ring molecular sieves listed above, and mixtures thereof. It is preferred that 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 therof.
• the metal hydrogenation component can be deposited on either the first dewaxing component, the second isomerization component or preferably on both the first and second components.
• the metal is selected from at least one of Group VIB and Group VIII, preferably Group VIII, more preferably Pt, Pd, and mixtures thereof.
• the amount of metal can range from 0.1 to 30 wt.%, based on catalyst. If the metal is Pt, Pd or a mixture thereof, the preferred amount is from 0.1 to 5 wt.%, based on catalyst. In order to maximize catalyst conversion, it is preferred that the metal dispersion be at least 0.3 if the metal is only on one component.
• the dispersion on one of the components be at least 0.3.
• the first and second components are combined in a ratio sufficient to promote wax isomerization and naphthene 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 (t-l,2/t-l,3 DMCP) in the range of less than about 1 have been found to promote maximum yields of basestocks.
• the second factor is when the catalyst, impregnated with about 0.5 wt.% Pt and evaluated in converting methyl cyclohexane to various cyclopentane compounds at 320° at 10% conversion, exhibits a selectivity for ethylcyclopentane (ECP) formation above at least 50%.
• ECP ethylcyclopentane
• the ratio of trans- 1 ,2-DCMP to trans- 1 ,3-DCMP is adjusted to less than about 1 predominantly by controlling the acidity of the amorphous isomerization component. It is preferred to use weakly acidic amorphous components such as alumina. Increasing the acidity of the amorphous phase generally increases the above-cited ratio.
• the hydroisomerization 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/m3) and a LHSV of 0.5 to 5 v/v/hr, preferably 1 to 2 v/v/hr.
• the wax 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 C 3 -C 6 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.
• liquified, 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.
• This example illustrates the yield -VI trade-off on a hydrocracker distillate (Feed A) for catalysts with different degrees of acidity in the amorphous component.
• the physical properties of the hydrocracker distillate (Feed A) are shown in Table 1.
• the catalyst in Table 2 (column C) was made by combining the zeolite TON with silica-alumina (Si-Al) using the same technique as used in column A to produce a homogeneous powdered catalyst before forming into pellets.
• the palladium was loaded (as palladium tetraamine dinitrate) on to the finished unitized catalyst by incipient wetness.
• Table 2 shows a comparison of activity and selectivity of these two catalysts for hydrodewaxing versus solvent dewaxing (column A).
• the acidity differences of each catalyst component and the corresponding finished unitized catalysts is also shown using the reaction of methylcyclohexane at 320°C.
• the table clearly shows the higher acidity (greater number and acid strength) silica-alumina catalyst (column C) gives lower yield but much higher VI compared with the very low acidity associated with alumina (column B) which results in high yield but a debit in VI.
• This example further illustrates the yield- VI trade off and shows a comparison of activity and selectivity of two catalysts for hydrodewaxing a hydrocraker distillate (Feed B) versus solvent dewaxing.
• the physical properties of the hydrocracker distillate (Feed B) are shown in Table 3.
• Wax Content wt% 22.4
• This example further illustrates the yield- VI trade and shows a comparison of activity and selectivity of two catalysts for hydroisomerization a hydrocraker distillate (Feed B) versus solvent dewaxing.
• This example illustrates that by changing the relative amounts of microporous component to amorphous component the overall acidity of the unitized catalyst an be tailored to maximize yield or VI.
• Table 5 compares two unitized catalysts both of which have been made by combining the powdered ZSM-5 (Si/Al ratio 110) with the powdered amorphous component in different ratios and then loading platinum by incipient wetness using platinum tetraamine dichloride.
• Table 5 shows a comparison of activity and selectivity for these catalysts for dewaxing hydrocracker Distillate B, the physical properties of which are shown in Table 3, with solvent dewaxing.
• the catalyst in column B which has a 1,2/1,3 DMCP ratio of ⁇ 1 shows higher yield but lower VI than the catalyst in column C which has a 1,2/1,3 DMCP ratio >1.
• the catalysts in Table 6 were made by combining the zeolite theta- 1 (TON) in the powder form with alumina (BET Surface Area 190m 2 /m 3 ) in the powder form followed by intimate mixing so as to form a homogeneous powdered mixture and then forming into catalyst pellets by pressing in a die and sizing to the required mesh size.
• TON zeolite theta- 1
• BET Surface Area 190m 2 /m 3 alumina
• Table 6 columns A and B, compares the activity of two TON zeolite/alumina mixed powder catalysts in which the noble metal has been loaded only on the TON zeolite component.
• the Pd TON/alumina catalyst (column B), which has 12% metal dispersion, is shown to have much lower activity for pour point reduction than the Pt TON/alumina catalyst (column A) which has 65 % metal dispersion.

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