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US20080149534A1 - Method of conversion of residues comprising 2 deasphaltings in series - Google Patents

Method of conversion of residues comprising 2 deasphaltings in series Download PDF

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US20080149534A1
US20080149534A1 US11/961,239 US96123907A US2008149534A1 US 20080149534 A1 US20080149534 A1 US 20080149534A1 US 96123907 A US96123907 A US 96123907A US 2008149534 A1 US2008149534 A1 US 2008149534A1
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deasphalting
fraction
solvent
hydroconversion
feed
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Thierry Gauthier
Serge Coatanea
Pierre Danial-Fortain
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IFP Energies Nouvelles IFPEN
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Assigned to INSTITUT FRANCAIS DU PETROLE reassignment INSTITUT FRANCAIS DU PETROLE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: COATANEA, SERGE, DANIAL-FORTAIN, PIERRE, GAUTHIER, THIERRY
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    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C

Definitions

  • the invention relates to the treatment of petroleum residues, resulting for example from the atmospheric distillation of a petroleum fraction. More precisely, it relates to hydrocarbon feedstock obtained from petroleum and having a boiling curve such that less than 10 wt. % of the fraction is distilled at a temperature of 343° C. in ambient conditions.
  • Petroleum residues are characterized by a molecular continuum that is difficult to characterize in detail.
  • the molecules are placed in groups defined by their affinity for solvents of increasing polarity (Jewell D. M., Albaugh E. W, Davis B E, and Ruberto R G, “Integration of chromatographic and spectroscopic techniques for the characterization of residual oils”, Ind. Eng. Chem. Fundam., 13, 3, 1974).
  • the “Saturates” fraction, the “Aromatics” fraction, the “Resins” fraction and the “Asphaltenes” fraction are defined. These fractions can be measured using techniques of liquid chromatography.
  • the petroleum residues contain heteroatoms.
  • large amounts of sulphur-containing compounds are found to be present (the S content is typically from 0.5 to 5%), nitrogen-containing compounds (typically, the nitrogen content varies from 0.05 to 1%), metals (Ni, V, possibly Fe etc.).
  • These heteroatoms are not distributed uniformly in all the fractions.
  • metals are found essentially in the “Asphaltenes” fraction and a small amount in the “Resins” fraction. However, they are absent from the “Saturates” and “Aromatics” fractions.
  • the nitrogen concentration is higher in the “Asphaltenes” and “Resins” fractions than in the “Saturates” and “Aromatics” fractions.
  • sulphur is distributed fairly uniformly in all the fractions.
  • the invention relates to a method of conversion of residues comprising at least four stages: a deasphalting of the residue in the presence of a heavy solvent (C5-C7), a second deasphalting in the presence of a light solvent (C3-C4), catalytic cracking of the fractions of the residue dissolved by the solvents in the two successive stages of deasphalting, and hydroconversion of the fractions of the residue that were not dissolved in the two successive stages of deasphalting.
  • a deasphalting of the residue in the presence of a heavy solvent C5-C7
  • a second deasphalting in the presence of a light solvent
  • catalytic cracking of the fractions of the residue dissolved by the solvents in the two successive stages of deasphalting catalytic cracking of the fractions of the residue dissolved by the solvents in the two successive stages of deasphalting
  • the heavy feedstock undergoes 2 successive deasphaltings, with mixtures of solvents that are preferably identical, one being a C3 hydrocarbon and the other a hydrocarbon with at least 5 carbon atoms.
  • the solvents used are identical for the 2 deasphaltings, with variable proportions.
  • the 1st deasphalting is carried out with a heavy mixture of solvents to precipitate the asphaltenes and the 2nd with a light mixture of solvents to precipitate the resins.
  • the deasphalted and deresined fraction is sent to catalytic cracking, the asphaltenes are not upgraded (used as solid fuel).
  • the aim of the present invention is to maximize the conversion of the residues in their entirety, i.e. also including the asphaltenes, the resins, the aromatics, and the saturated hydrocarbons, to produce light fractions and to upgrade the heavy fraction boiling above 540° C.
  • the crude undergoes atmospheric distillation, the residue is submitted to vacuum distillation and the vacuum residue constitutes the feed for the first deasphalting.
  • the present invention relates to a method of conversion of heavy oil feedstock with 5 wt. % boiling at least 343° C. and at least 40 wt. % of molecules boiling above 540° C., comprising:
  • the aim of the invention is therefore to propose a flowsheet in which the conversion is optimized by separating the residue beforehand into different fractions, said different fractions then being converted by the methods that are the most suitable. This results in a substantial gain in performance, the conversion being maximized and the yields and qualities of products in light fractions being improved.
  • fraction DARO containing most of the “Saturates” and “Aromatics” fractions, rich in hydrogen, with low metal content, less nitrogen and low content of coke precursors (asphaltenes), and the polyaromatic structures contained in the molecules are essentially constituted of 2 and 3 aromatic rings
  • fraction ASRES containing most of the “Resins and Asphaltenes” fractions, with high content of metals, nitrogen and coke precursors (asphaltenes) and low hydrogen content, and containing polyaromatic structures often containing more than 3 or 4 polyaromatic rings.
  • the fraction DARO is a fraction that can be converted advantageously by catalytic cracking (FCC).
  • FCC catalytic cracking
  • the fraction ASRES is a fraction that can only be converted in harsh conditions, and only hydroconversion can perform this operation efficiently.
  • Successive deasphalting in two stages the first being carried out by contacting with a heavy solvent (preferably C5-C7) and the second with a light solvent (preferably C3-C4), makes it possible to maximize the yield of fraction DARO rich in hydrogen (greater than or equal to 11 wt. %, preferably 11.5 wt. %), and with low content of metals ( ⁇ 40 ppm and preferably ⁇ 5 ppm) and of coke precursors (asphaltenes less than or equal to 1 wt. %, preferably ⁇ 0.5 wt. %).
  • a heavy solvent preferably C5-C7
  • a light solvent preferably C3-C4
  • the solvent in the first deasphalting is an n-paraffin having from 5 to 7 carbon atoms and the solvent in the second deasphalting is an n-paraffin having at least 3 or 4 carbon atoms.
  • the solvent in the first deasphalting is n-pentane and the solvent in the second deasphalting is propane or n-butane.
  • the deasphaltings are carried out in the range 30-40 bar (3-4 MPa).
  • the temperatures are generally between 45 and 130° C. for C3 and C4 solvents, more precisely, preferably between 45 and 90° C. for a C3 solvent and between 80 and 130° C. for a C4 solvent, and generally the temperatures are between 140 and 250° C. for C5 to C7 solvents and more precisely preferably between 140 and 210° C. for a C5 solvent and between 150 and 250° C. for a C6 or C7 solvent.
  • the ratio of solvent to deasphalting feedstock is generally between 5 and 10 for the C3 and C4 solvents, and more precisely preferably between 6 and 10 for a C3 solvent and between 5 and 8 for a C4 solvent, and generally the ratio is between 3 and 6 for C5 to C7 solvents.
  • the number of theoretical stages is generally at least 2 for the C3 and C4 solvents, and more precisely preferably at least 3 for a C3 solvent and between 2 and 3 for a C4 solvent, and generally between 1 and 2 for C5 to C7 solvents.
  • Fluidized-bed or slurry hydroconversion of the residues permits cracking at high temperature (400-480° C.) and at high hydrogen partial pressure (typically 50-150 bar) of residues in the presence of a metallic catalyst promoting hydrogenation of the cracked molecules.
  • a metallic catalyst promoting hydrogenation of the cracked molecules.
  • Continuous addition of catalyst makes it possible to maintain catalyst activity despite the presence of metals.
  • This method is suitable for the conversion of very heavy feedstock with high metal contents (typically 100-800 ppm), low hydrogen content and high contents of asphaltenes, the latter being converted by cracking and hydrogenation. This method requires long residence times. The capital expenditure associated with such a method is therefore high.
  • FCC and fluidized-bed or slurry hydroconversion are employed so as to optimize the economics of the method.
  • FCC produces a gasoline with a good octane number (Research Octane Number between 85 and 95 and Motor Octane Number between 75 and 85).
  • gas oil and the unconverted fractions are very aromatic (typically containing polycyclic aromatic structures with 2, 3 or 4 aromatic rings).
  • the cetane number of the gas oil is not very good, generally between 15 and 30.
  • These fractions additionally contain large amounts of sulphur.
  • the fractions heavier than gasoline can therefore be used advantageously as fluxes of the ASRES feedstock obtained from the two stages of deasphalting.
  • the aromatic cuts will make it possible to stabilize the asphaltenes and the resins in the reaction mixture, preventing flocculation of the latter before conversion and in the process effluents.
  • the gas oil from hydroconversion has a better cetane number than that from FCC, generally between 35 and 45.
  • the octane number of the gasoline is not so good, however.
  • the research octane number or motor octane number is generally close to 50.
  • the invention makes it possible to maximize the gasoline fractions produced by FCC and the gas oil fractions produced by hydroconversion. Therefore not only the conversion of the residue, but also the quality of the products formed, are maximized.
  • FIG. 1 method according to the invention
  • FIG. 2 method of the prior art in Example 2 route 1
  • FIG. 3 method with single deasphalting in Example 2 route 2
  • FIG. 4 method according to the invention, Example 2 route 3
  • FIG. 1 describes an example of application of the method of conversion of residues according to the present invention.
  • a petroleum feedstock (crude) ( 10 ) is distilled in atmospheric conditions and produces a substantial amount of a fraction ( 26 ) of atmospheric residue or ATR.
  • Fraction ( 26 ) is defined as the feed of the process according to the present invention. Generally it contains less than 10% of molecules distilling at 343° C. in these conditions and at least 40 wt. % boils above 540° C.
  • this feedstock is distilled under vacuum in a column ( 2 ), collecting a vacuum distillate ( 11 ), called VAD and a vacuum residue ( 12 ) called VAR.
  • VAD and VAR Fractions VAD and VAR are separated at a temperature varying, depending on the crudes, in a temperature range generally from 480 to 565° C.
  • the VAD fraction contains little or no metals Ni and V ( ⁇ 2 ppm) and the asphaltenes content of the feedstock is less than or equal to 1% and most often 0.5 wt. %. Its hydrogen content is greater than or equal to 11 wt. %, and most often 11.5%.
  • the VAR fraction contains most of the asphaltenes and metals contained in the feedstock ( 10 ).
  • the metals content (Ni+V) generally varies from 100 to 800 ppm, and the asphaltenes content varies from 2 to 25 wt. % depending on the feeds being processed. This fraction is of high viscosity (between 50 and 2000 cSt at 150° C., typically 400 cSt).
  • the VAR ( 12 ) is then sent to the first stage of deasphalting ( 3 ), in which the residue is contacted with a heavy solvent essentially constituted of saturated hydrocarbon molecules containing from 5 to 7 carbon atoms, preferably of n-pentane, n-hexane or n-heptane.
  • a heavy solvent essentially constituted of saturated hydrocarbon molecules containing from 5 to 7 carbon atoms, preferably of n-pentane, n-hexane or n-heptane.
  • ASPHALT phase 14
  • the solvent is separated by distillation of the soluble portions and recycled within the deasphalting process ( 3 ).
  • a soluble fraction ( 13 ) is obtained, called DAO fraction phase for “Deasphalted Oil” fraction.
  • This fraction ( 13 ) is then sent to the second stage of deasphalting ( 4 ), in which the residue is contacted with a light solvent, essentially constituted of saturated hydrocarbon molecules containing from 3 to 4 carbon atoms, preferably of n-propane or n-butane.
  • a light solvent essentially constituted of saturated hydrocarbon molecules containing from 3 to 4 carbon atoms, preferably of n-propane or n-butane.
  • two phases form: one constituted of the portions of the residue that are insoluble in the light solvent is called the RESIN phase ( 17 ); the other is constituted of the solvent and of the soluble portions of the residue.
  • the solvent is separated by distillation of the soluble portions and recycled within the deasphalting process ( 4 ).
  • the solvent-free soluble fraction ( 16 ) is called the DARO fraction phase for “DeAsphaltedResinsOil” cut.
  • the DARO fraction ( 16 ) contains small amounts of metals (Ni+V ⁇ 35 ppm) and of asphaltenes ( ⁇ 0.5 wt. %) which can vary depending on the solvent used. In a preferred embodiment of the invention and according to FIG. 1 , it is mixed with all of fraction ( 11 ) obtained from vacuum distillation ( 2 ) to produce the feed ( 18 ) of the fluidized-bed catalytic cracking (FCC) process ( 5 ).
  • the metals content is less than 20 ppm, preferably less than 5 ppm
  • the asphaltenes content is less than 0.4 wt. %, preferably 0.2 wt. %
  • the hydrogen content is greater than 11 wt. %, preferably 11.5 wt. %.
  • the characteristics of this feed are favourable for catalytic cracking.
  • the DARO prefferably treated by FCC, with the VAD fraction being treated by another process; according to another variant, the VAD is treated partly by FCC mixed with the DARO, the other portion being treated in some other way.
  • the catalytic cracking is carried out in a reaction zone containing a reaction chamber and a catalyst regeneration chamber, between which the catalyst circulates continuously.
  • the feed ( 18 ) is vaporized on contact with the hot regenerated catalyst and reacts with the catalyst in the reactor.
  • the temperature at the end of reaction is typically between 500 and 600°, preferably 520-540°, the ratio of the flow rate of catalyst to the flow rate of feed being between 4 and 15, preferably between 5 and 8.
  • the reaction products are then separated by distillation downstream from the reactor.
  • the catalyst is regenerated by combustion with air to remove the coke deposited during the reaction and reheat the catalyst. All the coke produced by cracking ( 22 ) is therefore consumed by combustion during regeneration.
  • the catalyst used for carrying out the cracking reaction is a catalyst based on silica alumina containing for example crystals of ultra-stable zeolite Y (USY) at a level of 10-40 wt. %.
  • the catalyst is finely divided to facilitate its circulation. Typically, the average diameter of the particles is between 50 and 100 microns.
  • the metals accumulate on the catalyst over time, and catalyst is added continuously in the process to keep the metals content limited to about 2000-15000 ppm on the catalyst, preferably 5000-10000 ppm.
  • the pressure at which cracking is carried out is generally less than 5 bar.
  • the liquid fractions heavier than gasoline ( 19 ) can be used partially or entirely, for fluxing (line ( 20 ) in FIG. 1 ) the fractions ASPHALT ( 14 ) and RESIN ( 17 ) produced in the two successive stages of deasphalting ( 3 ) and ( 4 ).
  • At least 50 wt. %, and preferably the whole, of the aromatic cuts boiling above 220° C. obtained in catalytic cracking is added to at least one of the precipitated fractions prior to hydroconversion. In this ways desulphurization is maximized and the quality of these aromatic cuts is improved.
  • the feed ( 15 ) thus constituted is treated in a process of hydroconversion of the residues ( 6 ), permitting the production of a fraction ( 29 ) rich in gases (H2S, NH3, C1, C2), a fraction C3-C4 ( 30 ), a gasoline fraction C5-220 ( 31 ), a gas oil fraction ( 32 ) (220-343° C.), a distillate fraction ( 33 ) (343-540° C.) and a residue fraction ( 34 ) 540° C.+ (the distribution between the fractions and the different cut points of the various effluents are given here purely indicatively).
  • the yield of gasoline can vary between 5 and 20 wt. % of the feed
  • the yield of gas oil can vary between 15 and 25 wt. % of the feed
  • the yield of distillates between 30 and 50 wt. % of the feed
  • the yield of residue from 5 to 50 wt. % of the feed.
  • Hydroconversion of the residues ( 6 ) is carried out in an assembly of one or more successive reactors, in conditions of high pressure (100 to 500 bar, preferably 150 to 250 bar), with a hydrogen partial pressure greater than 50 bar, preferably between 100 and 200 bar. Therefore hydrogen ( 28 ) is added continuously in the process, with the hydrogen consumption representing from 1 to 4 wt. % of the feed depending on the operating conditions.
  • This hydrogen can be obtained for example from natural gas reforming or from the gasification of coke or of residue.
  • the feed is introduced as a liquid into the reactors and is submitted to cracking at a temperature generally between 400 and 500° C., for a time between 1 and 10 h.
  • the catalyst can then be injected continuously in the feed upstream of the reactor and can be recovered from the effluents.
  • the catalyst can be a liquid containing at least molybdenum (for example molybdenum naphthenate or octoate, phosphomolybdic acid) precipitating as sulfides in the reactor, or a finely-divided solid (molybdenum deposited on alumina for example) the average particle size being less than 500 microns.
  • the catalyst is then injected in such a way that the molybdenum concentration is greater than 50 ppm in the feed.
  • the catalyst is supported, it is generally formed by extrusion, the diameter of the extrudates generally being greater than 0.75 mm.
  • the catalyst forms a fluidized bed in the reactors and is not entrained in the effluents. It generally contains at least 5 wt. % of molybdenum supported on alumina of very low acidity.
  • the catalyst is progressively laden with metals Ni, V originating from the feed. It is then necessary to add fresh catalyst continuously and withdraw used catalyst from the fluidized bed to compensate for the deactivation and maintain catalytic activity.
  • the content of metals derived from the feed ( 15 ) deposited on the catalyst can then reach between 10 and 150 wt. % of the catalyst depending on the conditions, the feedstock and the catalysts used.
  • the invention described in FIG. 1 includes a vacuum distillation column ( 2 ). It is also possible not to use vacuum distillation. In these conditions, the residue ( 26 ) supplies the first stage of deasphalting ( 3 ) directly and FCC ( 5 ) is supplied with a fraction originating essentially from the second stage of deasphalting.
  • distillate ( 11 ) produced in vacuum distillation ( 2 ) and the DARO fraction ( 16 ) obtained from the second stage of deasphalting can be treated separately, in two different catalytic cracking processes, or only treat fraction ( 16 ) in the FCC catalytic cracking process ( 5 ), the distillate then being upgraded differently, for example in a hydrocracking process.
  • the first example is intended to illustrate the advantage of using two successive stages of deasphalting first with a heavy solvent (C5-C7) and then a light solvent (C3-C4).
  • the feed chosen for illustrating this example is a vacuum residue obtained from a bitumen produced in the Athabaska region in the north of Canada.
  • the fraction DAO underwent a second deasphalting.
  • the role of the solvent was investigated.
  • Deasphalting of the DAO with n-butane was carried out with a solvent/feed ratio of 12/1 at a temperature of 100° C./80° C./60° C.
  • Deasphalting with n-propane was carried out with a solvent/feed ratio of 12/1 at a temperature of 70° C./55° C./45° C.
  • Table 1 summarizes the results obtained. The properties of the feed, of the DAO C7 obtained, of the DARO C4 and of the DARO C3 are shown, as well as the yields of the various fractions.
  • DARO C4 represents 45% of the starting residue
  • DARO C3 only represents 34%.
  • DARO C3 and C4 are therefore a priori potentially interesting feedstocks for FCC and are an important fraction of the residue. Double deasphalting, by selectively extracting the “Saturates” and “Aromatics” fractions, permits physical separation of the fractions, which can be converted by catalytic cracking.
  • a double deasphalting, coupling extraction with a heavy solvent with extraction with a light solvent therefore makes it possible to obtain a fraction of similar quality to that obtained by single deasphalting with the same light solvent, but at a far higher yield.
  • This atmospheric residue has an initial boiling point at 343° C. and contains 59 wt. % of molecules whose boiling point is above 540° C.
  • the vacuum distillation column operates in the same conditions.
  • the composition of the VAD and that of the VAR remain unchanged, the cut point being approx. 480° C.
  • Table 4 shows the composition of the feed of the FCC process in the 3 routes investigated. It can be seen that the feed is heavier when DAO C3 is integrated with VAD (route 2 ), or DARO C3 with VAD (route 3 ), as shown by the CCR (Carbon ConRadson; Conradson carbon value) of the fraction, which varies from 0.4 to 1.3. This will be reflected in an increase in production of coke, which is limited, however, and will mainly affect the thermal balance (temperature of regeneration and preheating in FCC). It can also be seen that the feed treated in FCC increases considerably on passing from route 1 , to route 2 and then to route 3 . The feed treated by FCC varies from 29.3% to 53.3% of the initial amount of atmospheric residue. However, the quality of the feed decreases somewhat, as shown by the densities, which change from 0.89 to 0.93, indicating that the feed becomes heavier.
  • CCR Carbon ConRadson; Conradson carbon value
  • Table 5 shows the composition of the feed of the hydroconversion process in the 3 routes investigated.
  • the amount of feed to be treated is least with double deasphalting.
  • the overall properties of the feed to be treated are very similar in the 3 routes, owing to introduction of the 220° C.+ fraction from FCC which fluxes the Asphalts or the Asphalts and the Resins, in increasing amounts as we pass from route 1 to route 2 and then to route 3 .
  • Table 6 describes the yields obtained in the 3 routes, relative to the amount of atmospheric residue treated. It shows the yields of H2S+NH3, of dry gases mainly containing H2, methane, ethane and ethylene, the C3-C4 fraction, the gasoline fraction C5-220° C., the gas oil fraction 220-343° C., the VAD fraction produced at 343-540° C., and the Residue fraction 540° C.+. It also shows the coke yield (consumed in the FCC unit) relative to the amount of atmospheric residue treated and the consumption of hydrogen in the hydroconversion unit, once again relative to the amount of atmospheric residue. The sum of the yields (the hydrogen consumption obviously being counted as negative) is very close to 100%.
  • route 1 and route 2 give quite similar overall conversion performance.
  • route 1 produces 48% of these bases whereas route 2 produces 49%.
  • Route 1 produces less C3-C4 fraction, less gasoline but more gas oil.
  • the overall conversion can be estimated from the amount of residual fractions 343° C.+. These values are close to 43%-45%. Note that the 540° C.+ fraction is greatly reduced as it now only represents 14%, against 59% in the starting feed.
  • Route 3 makes it possible to increase the conversion of the residue.
  • the production of C3-C4 fraction and of gasoline is increased, whereas the production of gas oil fraction remains similar to that obtained by route 2 .
  • the quantity of bases that can be upgraded (fraction C3-C4+fraction C5-220° C.+fraction 220° C.-343° C.) now represents 53%, or 4-5% more than routes 1 or 2 .
  • the residual fraction 343° C.+ represents 37%, or 6-8% less than routes 1 or 2 and the residual fraction of 540° C.+ drops to 11%, or 3% less than routes 1 or 2 .
  • Route 3 therefore offers better conversion of the atmospheric residue than routes 1 and 2 , producing larger amounts of gasoline.
  • the gasolines produced are of higher quality, since the proportion of gasoline from FCC in route 3 is 63%, against 53-55% for routes 1 and 2 , and the gasoline from FCC has a RON of 90 and a MON of 80 whereas that from hydroconversion is limited to 50 for RON and MON.
  • fractions C3-C4 which are more olefinic when they are obtained from FCC and therefore more upgradeable.
  • the quality of the gas oil fraction produced by route 3 will be better than the quality of the gas oil fraction produced by route 1 , with the whole of the gas oil fraction resulting from hydroconversion endowing the gas oil with a higher cetane number than FCC (40 against 25).

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FR0611.401 2006-12-21

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US20100329936A1 (en) * 2009-06-30 2010-12-30 Mark Van Wees Apparatus for integrating slurry hydrocracking and deasphalting
US20110142729A1 (en) * 2009-12-11 2011-06-16 Uop Llc Apparatus for producing hydrocarbon fuel
US20110139681A1 (en) * 2009-12-11 2011-06-16 Uop Llc Process for producing hydrocarbon fuel
US20110139676A1 (en) * 2009-12-11 2011-06-16 Uop Llc Composition of hydrocarbon fuel
US20130081977A1 (en) * 2011-08-31 2013-04-04 Exxonmobil Research And Engineering Company Hydroprocessing of heavy hydrocarbon feeds using small pore catalysts
US20130137909A1 (en) * 2011-07-27 2013-05-30 Christopher F. Dean Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
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CN106467760A (zh) * 2015-08-21 2017-03-01 中国石油化工股份有限公司 一种重油加工方法
WO2017117177A1 (fr) * 2015-12-28 2017-07-06 Exxonmobil Research And Engineering Company Désasphaltage séquentiel pour la production d'huile de base
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