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
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/20—Sulfiding
• • 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
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
  • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
  • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten 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
  • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
  • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
  • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
• • 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
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/0201—Impregnation
  • B01J37/0203—Impregnation the impregnation liquid containing organic compounds

Definitions

• the present invention relates to a process for effecting ultra-deep HDS of hydrocarbon feedstocks.
• ultra-deep HDS means the reduction of the sulfur content of a hydrocarbon feedstock to a value of less than about 200 ppm, preferably less than about 100 ppm, and even more preferably to a value of less than about 50 ppm, calculated by weight as elemental sulfur on the total liquid product, as determined in accordance with AST D-4294.
• the indications Group VIB and Group VIII correspond to the Periodic Table of Elements applied by Chemical Abstract Services (CAS system).
• a catalyst which comprises a Group VIB metal component, a Group VIII metal component, and an S-containing organic additive is particularly efficient in reducing the sulfur content of a hydrocarbon feedstock to a value of less than about 200 ppm.
• this catalyst may make it possible to effect this ultra-deep HDS in combination with at least one of improved reduction of the amount of nitrogen, improved reduction of the total amount of aromatics present, and improved reduction of the amount of polynuclear aromatics.
• the catalyst according to the invention shows ultra-deep HDS in combination with at least improved reduction of the amount of nitrogen, more preferably also in combination with improved reduction of the total amount of aromatics present, and improved reduction of the amount of polynuclear aromatics.
• the present invention is directed to a process for reducing the sulfur content of a hydrocarbon feedstock to a value of less than about 200 ppm, comprising optionally- subjecting a catalyst comprising a Group VIB metal component, a Group VIII metal component, and an S-containing organic additive on a carrier to a sulfidation step or activation step, and contacting a feedstock with a 95% boiling point of about 450°C or less with the optionally sulfided or activated catalyst under conditions of elevated temperature and pressure to form a product with a sulfur content of less than about 200 ppm.
• a catalyst comprising a Group VIB metal component, a Group VIII metal component, and an S-containing organic additive on a carrier to a sulfidation step or activation step, and contacting a feedstock with a 95% boiling point of about 450°C or less with the optionally sulfided or activated catalyst under conditions of elevated temperature and pressure to form a product with a sulfur content of
• the additive-containing catalyst can be any catalyst which comprises a Group VIB hydrogenation metal and/or a Group VIII hydrogenation metal, and an S-containing organic additive on a carrier. Catalysts comprising the combination of a Group VIB hydrogenation metal and a Group VIII hydrogenation metal are preferred.
• Catalysts which comprise a Group VIB metal component, a Group VIII metal component, and an S-containing organic additive are known in themselves in the art.
• European patent application No. 0 300 629 and European patent application No. 0 357 295 describe hydrotreating catalysts comprising a support impregnated with at least one member of molybdenum, tungsten, and/or metals of Group VIII of the Periodic Table, and a mercapto-compound selected from mercaptocarboxylic acids, amino-substituted mercaptanes, di-mercaptanes, and thioacids.
• the S-containing additive is incorporated into the catalyst composition to obviate the necessity of presulfiding, or to at least make the presulfiding less difficult.
• European patent application No. 0 506 206 also describes a hydrotreating catalyst comprising an S-containing additive selected from the group of bi- mercaptanes, aminosubstituted mercaptanes, and thiocarboxylic acids.
• the S- containing catalyst is again intended to avoid the necessity of presulfiding.
• Some of the catalysts described in this reference are activated by a treatment with hydrogen at a temperature from room temperature up to 400°C, preferably 100-300°C. Similar subject-matter is described in European patent application No. 0 338 788, and European patent application No. 0 289 211.
• US 5,139,990 describes a hydrotreating catalyst comprising a carrier and hydrogenation metal components which is treated with an aqueous medium comprising a water-soluble or water-miscible S-containing organic additive, followed by drying the resulting catalyst and activating it with hydrogen at a temperature of 100-600°C.
• US 4,636,487 describes a hydrotreating catalyst comprising a support and a hydroxymercaptide of one or more metals, which may be the reaction product of a mercaptoalcohol and one or more metal compounds.
• the catalyst may be activated with hydrogen at a temperature of 66-316°C.
• European patent application No. 0 496 592 describes a hydrotreating catalyst comprising a carboxylic acid and an organic sulfur compound which may be a mercaptocarboxylic acid.
• Group VIB metals suitable for use in the additive-containing catalyst for use in the process according to the invention may be mentioned molybdenum, tungsten, and chromium.
• Group VIII metals include nickel, cobalt, and iron. Catalysts comprising molybdenum as Group VIB metal component and nickel and/or cobalt as Group VIII metal component are preferred.
• catalysts comprising nickel may be preferred, especially when the feed comprises less than about 0.1 wt.% of sulfur.
• the catalyst usually has a metal content in the range of about 0.1 to about 50 wt.% calculated as oxides on the dry weight of the catalyst not containing the additive.
• the Group VIB metal will frequently be present in an amount of about 5 to about 40 wt.%, preferably about 15 to about 30 wt.%, calculated as trioxide.
• the Group VIII metal will frequently be present in an amount of about 1 to about 10 wt.%, preferably about 2 to about 7 wt.%, calculated as monoxide.
• the catalyst may also contain other components, such as phosphorus, halogens, and boron. Particularly, the presence of phosphorus in an amount of about 1 to about 10 wt.%, calculated as P 2 O 5 , may be preferred.
• the catalyst carrier may comprise the conventional oxides, e.g., alumina, silica, silica-alumina, alumina with silica-alumina dispersed therein, silica-coated alumina, magnesia, zirconia, boria, and titania, as well as mixtures of these oxides.
• alumina silica, silica-alumina, alumina with silica-alumina dispersed therein, or silica-coated alumina.
• the carrier consisting essentially of alumina or alumina containing up to about 25 wt.% of other components, preferably silica.
• a carrier comprising a transition alumina for example an eta, theta, or gamma alumina is preferred within this group, with a carrier comprising gamma-alumina being especially preferred.
• the catalyst may contain 0 to about 60 wt.% of zeolite.
• the catalyst's pore volume (measured via N2 adsorption)) generally is in the range of about 0.25 to about 1 ml/g.
• the specific surface area will generally be in the range of about 50 to about 400 m 2 /g (measured using the BET method).
• the catalyst will have a median pore diameter in the range of about 7 to about 20 nm, as determined by N2 adsorption.
• the figures for the pore size distribution and the surface area given, above are determined after calcination of the catalyst at 500°C for one hour.
• the catalyst is suitably in the form of spheres, pellets, beads, or extrudates.
• suitable types of extrudates have been disclosed in the literature (see, int. al., US 4,028,227). Highly suitable are cylindrical particles (which may be hollow or not) as well as symmetrical and asymmetrical polylobed particles (3 or 4 lobes).
• the additive present in the catalyst may be any S-containing organic additive.
• organic additive refers to an additive comprising at least one carbon atom and at least one hydrogen atom.
• Preferred compounds include the mercaptocarboxylic acids represented by the general formula HS-R1-COOR, wherein R1 stands for a divalent hydrocarbon group with 1 to about 10 carbon atoms and R stands for a hydrogen atom, an alkali metal, an alkaline earth metal, ammonium, or a linear or branched alkyl group having 1 to about 10 carbon atoms.
• Examples include mercaptoacetic acid (HS-CH2-COOH), beta-mercaptoproprionic acid (HS-CH2CH2-COOH), methylmercaptoacetate (HS-CH2-COOCH3), ethyl 2-mercaptoacetate (HS- CH2-COOC2H5), ethylhexyl mercaptoacetate (HS-CH2-COOC8H17), and methyl 3-mercaptoproprionate (HS-CH2CH2-COOCH3).
• Preferred compounds also include amino-substituted mercaptanes represented by the general formula H2N-R2-SH, wherein R2 stands for a divalent hydrocarbon group having 1 to about 15 carbon atoms.
• Examples of these compounds include 2-amino ethanethiol (H2N-CH2CH2-SH), and 4-amino thiophenol (H2N-C6H4-SH).
• Preferred compounds also include di-mercaptanes represented by the general formula HS-R3-SH, wherein R3 stands for a divalent hydrocarbon group having 1 to about 15 carbon atoms.
• Examples of these compounds include ethanedithiol (HS-CH2CH2-SH) and 1 ,4-butanedithiol (HS-(CH2)4-SH).
• Preferred compounds also include thioacids of the formula R4-COSH, wherein R4 stands for a monovalent hydrocarbon group having 1 to about 15 carbon atoms.
• Examples of these compounds include thioacetic acid (CH3-COSH) and thiobenzoic acid (C6H5COSH).
• Dithioacids of the formula HSOC-R5-COSH wherein R5 is a divalent hydrocarbon group with 1 to about 15 carbon atoms may also be suitable.
• An example is dithioadipic acid (HSOC-C4H10-COSH).
• Preferred compounds also include mercaptoalcohols of the general formula R6S-R5-(OH)n, wherein R5 represents an alkyl group having from 1 to about 15 carbon atoms or a phenyl group, R6 represents a hydrogen atom or an alkyl group having 1 or about 2 carbon atoms, and n is 1 or about 2.
• Examples of these compounds include 2-mercaptoethanol, 2-(methylthio)ethanol, 2- (ethylthio)ethanol, 3-mercapto-2-butanol, 4-mercaptophenoi, 2- (methylthio)phenol, 4-(methylthio)phenol, 2-(ethylthio)phenol, 3-mercapto-1 ,2,- propanediol, 3-methylthio-1 ,2, propanediol, and 3-ethylthio-1 ,2, propanedioi.
• Other suitable compounds include sulfoxides of the formula R7-SO-R8, wherein R7 and R8 are hydrocarbon groups with 1 to about 5 carbon atoms. An example is dimethyl sulfoxide (CH3-SO-CH3).
• Ammonium thiocyanate and thiourea may also be useful compounds, as may be the various dithiocarbamic acids and the salts thereof, such as ethylene bisdithiocarbamic acid and its salts, and dimethyl dithiocarbamic acid and its salts.
• Other suitable compounds include mercaptodiathiazoles and their salts, such as 2,5-dimercapto-1 ,3,4,-diathiazoles and its salts.
• R9-Sx- R10 Other compounds which may be useful are (poly)sulfides of the formula R9-Sx- R10, wherein x is a value of 1 to about 15 and R9 and R10 are alkyl groups, preferably branched alkyl groups, with 1 to about 30 carbon atoms.
• Related compounds are those with the formula HO-R11-Sx-R12-OH, wherein x is a value of 1 to about 15 and R11 and R12 are alkyl groups with 1 to about 8 carbon atoms.
• mercaptocarboxylic acids are considered preferred for reasons of activity.
• Other compounds in particularly those which are soluble in or miscible with water, may be preferred for environmental reasons (less odour and/or no organic solvent necessary).
• a single compound as well as a combination of compounds may be used as additive.
• the amount of additive present in the additive-containing catalyst depends on the specific situation. It was found that the appropriate amount of additive generally lies in the range of about 0.01 to about 2.5 moles of additive per mole of hydrogenation metals present in the catalyst. If the amount of additive added is too low, the advantageous effect associated with its presence will not be obtained. On the other hand, the presence of an exceptionally large amount of additive will not improve its effect.
• the aim is to select the amount of sulfur incorporated into the catalyst by way of the additive to correspond to about 5 to about 200%, preferably about 50 to about 200%, more preferably about 80 to about 150%, of the stoichiometric sulfur quantity necessary to convert the hydrogenation metals into Co 9 S 8 , MoS 2 , WS 2 , and Ni 3 S 2 , respectively.
• the way in which the additive is incorporated into the catalyst composition is not critical to the process according to the invention.
• the additive may be incorporated into the catalyst composition prior to, subsequent to, or simultaneously with the incorporation of the hydrogenation metal components.
• the additive can be incorporated into the catalyst composition prior to the hydrogenation metal components by being added to the carrier before the hydrogenation metal components are. This can be done by mixing the additive with the carrier material before it is shaped, or by impregnating the shaped carrier material with the additive. This embodiment is not preferred at this point in time.
• the additive can be incorporated into the catalyst composition simultaneously with the hydrogenation metal components. This can be done, e.g., by mixing the additive and the hydrogenation metal components with the carrier material before shaping or by impregnating the carrier with an impregnation solution comprising the hydrogenation metal components and the additive, followed by drying under such conditions that at least part of the additive is maintained in the catalyst. It is also possible to incorporate the additive into the catalyst composition subsequent to the hydrogenation metal components.
• the additive may be used in the solid form, in the liquid form, or dissolved in a suitable solvent. It may be preferred for the additive to be incorporated into the catalyst dissolved in water.
• the catalyst may be activated by contacting it with hydrogen at a temperature of about 100 to about 600°C as described in, e.g., EP 0 506 206, EP 0 338 788, EP 0 289 211 , US 4,636,487, and US 5,139,990.
• the catalyst may be contacted with an organic liquid either prior to or simultaneously with the contacting with hydrogen.
• Such a process is the subject of non- prepublished International patent application No. PCT/EP01/03877, which is incorporated herein by reference.
• the catalyst may be subjected to a sulfiding step before its use in effecting ultra-deep HDS, said sulfiding step taking place ex situ, in situ or in a combination of ex situ and in situ.
• the indication sulfiding step or sulfidation step is meant to include any process step in which a sulfur-containing compound is added to the catalyst composition and in which at least a portion of the hydrogenation metal components present in the catalyst is converted into the sulfidic form, either directly or after an activation treatment with hydrogen.
• Suitable sulfidation processes are known in the art. Ex situ sulfidation processes take place Outside the reactor in which the catalyst is to be used in hydrotreating hydrocarbon feeds. In such a process the catalyst is contacted with a sulfur compound, e.g. a polysulfide or elemental sulfur, outside the reactor and, if necessary, dried. In a second step, the material is treated with hydrogen gas at elevated temperature in the reactor, optionally in the presence of a feed, to activate the catalyst, i.e. bring it into the sulfided state. In situ sulfidation processes take place in the reactor in which the catalyst is to be used in hydrotreating hydrocarbon feeds.
• a sulfur compound e.g. a polysulfide or elemental sulfur
• the catalyst is contacted in the reactor at elevated temperature with a hydrogen gas stream mixed with a sulfiding agent, such as hydrogen sulfide or a compound which under the prevailing conditions is decomposable into hydrogen sulfide.
• a sulfiding agent such as hydrogen sulfide or a compound which under the prevailing conditions is decomposable into hydrogen sulfide.
• a hydrogen gas stream combined with a hydrocarbon feed comprising a sulfur compound which under the prevailing conditions is decomposable into hydrogen sulfide.
• a hydrocarbon feed comprising an added sulfiding agent a so-called spiked feed
• a sulfur-containing hydrocarbon feed without any added sulfiding agent, since the sulfur components present in the feed will be converted into hydrogen sulfide in the presence of the catalyst.
• the hydrocarbon feed may be the feed to be subjected to ultra-deep HDS in the process according to the invention, but it may also be a different feed, later to be replaced with the feed to be subjected to ultra-deep HDS. Combinations of the various sulfiding techniques may also be applied. In the context of the present invention it may be preferred to sulfide the catalyst by contacting it with an, optionally spiked, hydrocarbon feed.
• a further process for presulfiding catalysts comprising an organic S-containing catalyst is the subject of non-prepublished International patent application No. PCT/EP01/03895, which is incorporated herein by reference.
• This patent application is directed to a presulfiding process in which a catalyst comprising a sulfur-containing additive is presulfided in two steps, the first step being carried out at a lower temperature than the second step.
• Non-prepublished International patent application No. PCT/EP01/03843 which is incorporated herein by reference, also describes a suitable presulfiding procedure for catalysts containing an S-containing additive. In the process described in this reference the presulfiding is carried out ex-situ.
• the feedstock suitable for use in the process according to the invention has a 95%o boiling point, as determined in accordance with ASTM D-2887, of about 450°C or less, preferably about 420°C or less, more preferably about 400°C or less. That is, 95 vol.% of the feedstock boils at a temperature of about 450°C or less, preferably about 420°C or less, more preferably about 400°C or less.
• the initial boiling point of the feedstock is above about 100°C, preferably above about 180°C.
• the feedstock to be used in the process according to the invention may or may not have been subjected to a previous hydrodesulfurisation step, depending on the envisaged process conditions.
• the catalyst used in the process of the invention is sufficiently active to be able to convert fractions with " a sulfur content of, e.g., about 0.1 wt.% ppm to about 2 wt.%, preferably 1 to about 2 wt.%, into product with a sulfur content less than about 200 ppm, preferably less than about 100 ppm, more preferably, less than about 50 ppm.
• feedstocks generally contain about 20 to about 1200 ppm nitrogen, preferably about 30 to about 800 ppm, more preferably about 70 to about 600 ppm.
• the metal content of such feedstocks preferably is less than about 5 ppm, more preferably less than about 1 ppm (Ni+V).
• suitable feedstocks of this type are feedstocks comprising one or more of straight run gas oil, light catalytically cracked gas oil, and light thermally cracked gas oil, and (mild) hydrocracked oils.
• the invention is also suitable for the ultra-deep hydrodesulfurisation of hydrocarbon feeds of the above description which had already been subjected to a hydrotreating operation, and which have sulfur contents of generally less than about 0.1 wt.%, more specifically about 150 to about 500 ppm.
• hydrodesulfurisation hydrodesulfurisation
• a first hydrotreating (hydrodesulfurisation) step to reduce its sulfur content to a value less than about 0.1 wt.%
• This can be carried out in various ways.
• One can, e.g., use a conventional hydrodesulfurisation catalysts comprising a Group VIB metal component, a Group VIII metal component, and, optionally, phosphorus on a carrier comprising alumina.
• Suitable hydrodesulfurisation catalysts are commercially available, and include for example KF 756 and KF 901 of Akzo Nobel.
• first hydrodesulfurisation step by means of a two-step process, such as those described in EP 0 464 931 , EP-A 0 523 679 or EP 870 807. If so desired, one may also use an additive-based catalyst to effect such first hydrodesulfurisation step.
• the present invention also pertains to a two-step process for converting a starting feedstock having a sulfur content of above about 0.1 wt.% into a product having a sulfur content of less than about 200 ppm, wherein the process comprises optionally sulfiding and/or activating a first and a second catalyst comprising a Group VIB metal component and a Group VIII metal component, with at least the second catalyst additionally comprising an S- containing organic additive, contacting a feedstock with a 95% boiling point of about 450°C or less and a sulfur content of about 0.1 wt.% or more with the first catalyst under conditions of elevated temperature and pressure to form a product with a sulfur content of less than about 0.1 wt.%, preferably less than about 500 ppm, and contacting the effluent from the first catalyst, optionally after fractionation or intermediate phase separation, with the second catalyst under conditions of elevated temperature and pressure to form a product with a sulfur content of less than about 200 ppm, preferably less than about 100 pp
• the first catalyst prefferably comprises molybdenum as Group VIB metal component and cobalt and/or nickel as Group VIII metal component
• the second catalyst comprising molybdenum as Group VIB metal component and nickel as Group VIII metal component.
• the two-step process can be carried out in one or two reactors, as may be desired. If both catalysts contain an organic additive, the two catalysts may be the same or different.
• the process according to the invention is carried out at elevated temperature and pressure.
• the temperature generally is about 200 to about 450°C, preferably about 280 to about 430°C.
• the reactor inlet hydrogen partial pressure generally is about 5 to about 200 bar, preferably about 10 to about 100 bar, more preferably about 15 to about 60 bar.
• the liquid hourly space velocity preferably is between about 0.1 and about 10 vol./vol.h, more preferably between about 0.5 and about 4 vol. vol.h.
• the H 2 /oil ratio generally is in the range of about 50 to about 2000 Nl/I, preferably in the range of about 80 to about 1000 Nl/I.
• the reaction conditions for both steps may be selected independently from each other, taking the above-mentioned general and preferred ranges into acccount.
• the process conditions are selected in such a way that the sulfur content of the total liquid effluent is less than about 200 ppm, preferably less than about 100 ppm, more preferably less than about 50 ppm.
• the exact process conditions will depend, int. al., on the nature of the feedstock, the desired degree of hydrodesulfurisation, and the nature of the catalyst. In general, a higher temperature, a higher hydrogen partial pressure, and a lower space velocity will decrease the sulfur content of the final product.
• the selection of the appropriate process conditions to obtain the desired sulfur content in the product is well within the scope of the person skilled in the art of hydroprocessing.
• Extrudates of a gamma-alumina carrier were impregnated to pore volume saturation with an impregnation solution comprising a molybdenum compound, a nickel compound, and phosphoric acid, after which the impregnated carrier was dried at a temperature of 140°C for a period of 16 hours.
• the dried extrudates were impregnated with a solution of thioglycolic acid (TGA), and dried.
• TGA thioglycolic acid
• the final catalyst contained 20 wt.% of molybdenum, calculated as trioxide, 5 wt.% of nickel, calculated as oxide, and 7 wt.% of phosphorus, calculated as P 2 0 5 . All weight percentages are calculated on the dry catalyst base, not including the additive.
• the molar ratio between TGA and the total of Ni and Mo is 0.4.
• the catalyst according to the invention was tested in an upflow tubular reactor side by side with commercial catalyst KF 756 of Akzo Nobel. Each reactor tube contained 75 ml of catalyst homogeneously intermixed with 70 ml of carborundum particles. The catalysts were sulfided using the feed specified below in which dimethyl disulfide had been dissolved to a total S content of 2.5 wt.%.
• the feed applied was a Kuwait petroleum gas oil feedstock with the following properties.

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• 2001
  • 2001-08-20 EP EP01962959A patent/EP1322730A1/de not_active Withdrawn
  • 2001-08-20 AU AU2001284027A patent/AU2001284027A1/en not_active Abandoned
  • 2001-08-20 WO PCT/EP2001/009641 patent/WO2002020702A1/en not_active Ceased
  • 2001-08-20 JP JP2002525710A patent/JP2004508453A/ja active Pending
  • 2001-08-30 US US09/942,830 patent/US20020070147A1/en not_active Abandoned

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