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
• • 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
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/85—Chromium, molybdenum or tungsten
  • B01J23/88—Molybdenum
  • B01J23/882—Molybdenum and cobalt
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
  • B01J27/04—Sulfides
  • B01J27/047—Sulfides with chromium, molybdenum, tungsten or polonium
  • B01J27/051—Molybdenum
  • B01J27/0515—Molybdenum with iron group metals or platinum group metals
• • 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

Definitions

• the present invention relates to the field of hydrotreating hydrocarbon feedstocks and more particularly relates to a process for the sulfurization of catalysts used for this purpose.
• hydrotreatment catalysts of hydrocarbon feedstocks concerned by the present invention, are used under suitable conditions for converting, in the presence of hydrogen, the organosulfur compounds into hydrogen sulfide, an operation which is called hydrodesulfurization (HDS), and for converting the organo-nitrogen compounds in ammonia in a process called hydro-denitrogenation (HDN).
• HDS hydrodesulfurization
• HDN hydro-denitrogenation
• These catalysts are generally based on metals of groups VI B and VIII of the periodic table of elements, such as molybdenum, tungsten, nickel and cobalt.
• the most common hydrotreatment catalysts are formulated from cobalt-molybdenum (Co-Mo), nickel-molybdenum (Ni-Mo) and nickel-tungsten (Ni-W) systems, deposited on porous mineral supports such as aluminas, silicas, silica-aluminas.
• Co-Mo cobalt-molybdenum
• Ni-Mo nickel-molybdenum
• Ni-W nickel-tungsten
• the method mainly used in the past by refiners consisted of sulfurizing the catalysts with sulfur-containing petroleum feedstocks, but this technique had significant drawbacks because of the difficulty of transforming the sulfur-containing compounds into hydrogen-sulfur.
• the sulfurizations started at low temperature, had to be carried out slowly to obtain complete sulfurization of the catalysts at high temperature.
• Sulfur additives have been proposed to improve the sulfurization of the catalysts.
• the method consists in incorporating a sulfur compound (spiking agent) into a filler such as a naphtha or into a particular cut such as a VGO (vacuum gas oil) or an LGO (light gas oil).
• This operation has the effect of eliminating the organic solvent and ensuring the fixing of the sulfur to the catalyst via the organic polysulphides.
• the catalyst is stable in air and can be handled without special precautions. It is supplied in this state to the user who, after loading into the hydrotreatment reactor, can complete the sulfurization of the catalyst under hydrogen for the total transformation of metals into metal sulfides.
• the catalyst is introduced into the hydrotreatment reactor in oxide form and is sulfurized in the presence of the sulfurizing agent under a stream of hydrogen as opposed to "ex situ" presulphurization where the catalyst is presulphurized in outside the hydrotreatment reactor.
• the present invention now relates to a particular mode of implementation "in situ" of this tertiary mercaptan. It has indeed been found, surprisingly, that the prior "in situ” introduction of the tertiary mercaptan in the absence of hydrogen, followed by the subsequent introduction into the same reactor of the other sulfurizing agent (for example, dimethyldisulfide) in the presence of hydrogen this time, also made it possible to obtain significantly more active catalysts than those sulfide with dimethyldisulfide alone.
• the other sulfurizing agent for example, dimethyldisulfide
• the subject of the invention is therefore a process for the in situ sulfurization of a metal hydrotreatment catalyst comprising a step of treating the catalyst with a tertiary mercaptan in the absence of hydrogen, followed in the same reactor by a step of treatment with another sulfurizing agent in the presence of hydrogen.
• the tertiary mercaptans relating to the present invention are the same as those mentioned in patent FR 2 758 478 and correspond to the general formula:
• R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 and R 8 identical or different, each represent a hydrogen atom or an alkyl radical, linear or branched, aryl, alkylaryl or aralkyl, these radicals being able to contain one or more heteroatoms such as oxygen and / or sulfur.
• the preferred tertiary mercaptans of the invention are those which contain from 4 to 16 carbon atoms. Such mercaptans are manufactured industrially from hydrogen sulphide and olefins by catalytic processes such as those described in particular in US patents 4,102,931, EP 101,356 and EP 329,521. Tertiobutylmercaptan (TBM) is thus manufactured at from isobutene, tertiononylmercaptan (TNM) from tripropylene and tertiododecylmercaptan (TDM) from tetrapropylene or triisobutylene. CT is the most particularly preferred tertiary mercaptan.
• the first step of the process according to the invention essentially consists in incorporating the tertiary mercaptan in the pores of the catalyst and in subjecting the catalyst thus impregnated to thermal activation. under an atmosphere of an inert gas (for example, nitrogen or methane).
• an inert gas for example, nitrogen or methane
• the impregnation of the catalyst it is possible to use pure tertiary mercaptan, but it is advantageous to use it in the form of a solution in an organic solvent (preferably an alkane or a desulfurized gas oil) the concentration in tertiary mercaptan of this solution which can vary within wide limits depending on the nature of the tertiary mercaptan, its sulfur content and the pore volume of the catalyst to be sulfurized.
• an organic solvent preferably an alkane or a desulfurized gas oil
• the first method when the pore volume is saturated, consists in passing a volume of solution comprising the tertiary mercaptan and the organic solvent described above in the desired proportions over the catalyst.
• the volume of this solution corresponds to the total pore volume of the mass of catalyst.
• This volume is then slightly increased to take account of the inert wetting volume (SiC - Carborundum) which is placed before the catalyst.
• the second method by recirculation, consists in circulating in a loop a volume of solution comprising the tertiary mercaptan and the organic solvent in the desired proportions on the catalyst. This volume of solution is greater than the total pore volume of the mass of catalyst. Analysis over time shows that the recycled solution depletes tertiary mercaptan and that it is retained by the catalyst.
• the thermal activation is carried out at a temperature which can range from 50 to 250 ° C., but is preferably between 100 and 175 ° C.
• the pressure is not a critical parameter and can range from atmospheric pressure up to 35 bars.
• the sulfur compounds to be used as sulfurizing agents in the second step of the process according to the invention can be of different types: feed to be desulphurized, carbon sulphide, light mercaptans (for example, ethyl mercaptan and n-butyl mercaptan), dimethyl sulphide, dimethyldisulphide (DMDS), and optionally polysulfides such as ditertiononylpolysulfide or ditertiobutylpolysulfide; can also be used polysulfides obtained from sulfur and olefins.
• DMDS is the most particularly preferred sulfurizing agent.
• This sulfurization agent is generally introduced in mixture with a diesel fuel, under a hydrogen pressure which can range from atmospheric pressure up to 200 bars, but is preferably between 10 and 50 bars, pressure range commonly used industrially.
• This second step of the process according to the invention (in situ treatment of the catalyst with the other sulfurizing agent in the presence of hydrogen) is carried out at a temperature which can range up to 350 ° C .; a higher temperature would reduce the sulfurization time, but would increase the risk of coking. It is advantageous to carry out this second stage in two stages:
• the hydrogen coverage expressed by the ratio of the volume flow rate of hydrogen in normal liters to the volume flow rate of diesel fuel in liters can be between 50 and 500 Nl / I, preferably between 100 and 300 Nl / I.
• the hourly space velocity (WH), defined as the ratio between the hourly volume flow of diesel fuel and the volume of catalyst, can range from 0.1 to 5 h “1 and is preferably between 1 and 3 h "1 , the interval commonly used industrially.
• the total amount of sulfur supplied by the tertiary mercaptan and the other sulfurizing agent can range from 100 to 250% of the weight of sulfur stoichiometrically required for the total conversion of the oxides of the catalyst to sulphides.
• the proportion of tertiary mercaptan, used in the implementation of the process according to the invention, can represent from 1 to 100% of the weight of total sulfur necessary for the sulfurization of the catalyst.
• the sulfur provided by the tertiary mercaptan has a particularly sensitive effect from 10% by weight of the total sulfur necessary for the sulfurization of the catalyst.
• Examples 1 and 2 presented are to show the gains in catalytic activity which can be obtained in a hydrotreatment test reaction, hydrodesulfurization (HDS) of thiophene, with an industrial catalyst Co-Mo / alumina which has been subjected to in-situ sulfurization under conventional sulfurization conditions (Example 1) and in-situ sulfurization under conditions specific to the present invention (Example 2).
• the purpose of Examples 3 and 4 is to illustrate the in-situ impregnation of the catalyst with tertiary mercaptan according to the recirculation method.
• the catalyst used is a commercial hydrodesulfurization catalyst (KF756 from the company AKZO), consisting of cobalt and molybdenum oxides supported on alumina and having the following characteristics: - form: four-lobe
• the operation was carried out in a reactor (internal volume: 120 ml) placed in an oven with three heating zones and provided at its outlet with a device making it possible to separate the liquid phase and the gas phase and to recycle them.
• a sampler is used to collect liquids in order to determine the total sulfur level present in the diesel fuel and then to carry out analyzes by gas chromatography.
• 30 g of catalyst (approximately 40 ml) were introduced between two layers of carborundum (SiC), an inert agent which promotes the wetting of the catalyst and which also serves as a thermal buffer.
• SiC carborundum
• the catalyst was wetted with a diesel fuel obtained from the atmospheric distillation of crude oil (Straight Run GasOil; hereinafter SRGO) and having the characteristics gathered in the following table:
• the hydrodesulfurization reaction of the thiophene was carried out at atmospheric pressure according to the following operating protocol: The temperature of the reactor is maintained at 400 ° C., while a mixture
• H2S-H2 with an H2S content of 2% by volume and a gas flow rate set at 5.4 l / h is introduced into the reactor.
• the hydrogen is sent to a saturator containing the liquid thiophene thermostatically controlled at a temperature such that the partial pressure of the thiophene in the gas entering the reactor is 60 torr (8 kPa).
• the gaseous effluents leaving the reactor are analyzed by chromatography to determine the unconverted thiophene and the C 4 hydrocarbons formed. The reaction is followed for 3 hours with periodic analyzes of the gaseous effluents.
• the evaluation of the activity of the catalyst for the hydrodesulfurization test reaction is determined by the rate of disappearance of the thiophene under these conditions.
• this reference test has been assigned a relative activity expressed in RVA (Relative Volumic
• RVA 100 xk / k ref of 126.
• the solution is recirculated in an up-flow with respect to the catalytic bed with a flow rate of 80 cm 3 / h, under a nitrogen flow of 20 l / h at a pressure of 4 bars, and with a temperature rise of 50 ° C / h up to a plateau temperature of 150 ° C.
• the analysis of the liquid recycle shows that 83%> of the TDM initially present reacted on the catalyst.
• the solution is recirculated in up-flow relative to the catalytic bed with a flow rate of 80 cm3 / h, under a nitrogen flow of 20 l / h at a pressure of 4 bar, and with a temperature rise of 50 ° C / h up to a plateau temperature of 120 ° C.
• the 120 ° C level is maintained for 1.5 hours, then with a rise of 50 ° C / h, a second level of 135 ° C is reached which is maintained for 2 hours.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Materials Engineering (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Catalysts (AREA)

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• 2001
  • 2001-02-22 FR FR0102410A patent/FR2820991B1/fr not_active Expired - Fee Related
• 2002
  • 2002-02-13 KR KR10-2003-7011028A patent/KR20030080228A/ko not_active Application Discontinuation
  • 2002-02-13 EP EP02706852A patent/EP1361923A1/fr not_active Ceased
  • 2002-02-13 US US10/468,936 patent/US20040112795A1/en not_active Abandoned
  • 2002-02-13 JP JP2002565711A patent/JP2004528962A/ja active Pending
  • 2002-02-13 WO PCT/FR2002/000548 patent/WO2002066161A1/fr not_active Application Discontinuation
  • 2002-02-13 CA CA002438536A patent/CA2438536A1/fr not_active Abandoned
  • 2002-02-22 AR ARP020100627A patent/AR032838A1/es not_active Application Discontinuation

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