Classifications

• • 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
  • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
  • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
  • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
  • C10G67/0454—Solvent desasphalting
  • C10G67/0463—The hydrotreatment being a hydrorefining

Definitions

• the instant invention describes a process for upgrading heavy feeds utilizing a process wherein solvent deasphalting precedes a hydroprocessing step.
• U.S. 3,896,025 teaches hydrocracking of a crude petroleum lubricating oil to improve its viscosity index.
• the feed may be obtained from a deasphalted vacuum residuum.
• U.S. 3,929,616 teaches solvent refining a heavy resid followed by hydrocracking the resulting raffmate and deasphalting of a fraction of the hydrocracked product.
• U.S. 4,030,429 and U.S. 5,601,697 teach solvent deasphalting followed by cracking.
• U.S. 5,024,750 and U.S. 4,940,529 teach catalytic cracking of solvent deasphalted oils obtained from hydrotreated heavy oils.
• U.S. 4,405,441 teaches hydrotreating followed by cracking and deasphalting.
• U.S. 4,400,264 teaches cracking followed by hydrotreating and deasphalting.
• U.S. 4,500,416 teaches deasphalting of an asphaltenes-containing feed followed by hydrotreatment and thermal cracking of the asphalt fraction.
• the hydrotreatment process preferably includes a pre- treatment step to remove metals which poison the catalyst.
• the deasphalting step is conducted on an asphaltenes-containing hydrocarbon mixture.
• the hydrotreated portion is then used to produce one or more distillate fractions or heavy fractions.
• An embodiment of the instant invention is directed to a process for upgrading a non-hydrotreated feedstream, said process comprising:
• upgraded oil recovered from the hydroprocessed product in step (c) is combined with the deasphalted oil of step (a) to obtain a finished upgraded crude.
• the separation step (c) can be achieved by any means known to the skilled artisan.
• the hydroprocessed product can undergo a second solvent deasphalting step in the same (as in step (a)) or a stand alone deasphalter or a distillation step to provide a liquid product with boiling point below about 1025°F and residue boiling above about 1025°F.
• the 1025-°F liquid or deasphalted oil obtained from the second solvent deasphalting step may then be combined with the deasphalted oil of step (a) to obtain a finished upgraded crude.
• the 1025+°F may be combined with the asphalt fraction from the first SDA step or used directly as boiler fuel or as feed to a coker or a partial oxidation (POX) unit.
• POX partial oxidation
• step (a) The asphalt product of step (a) is oftentimes referred to in the art as "rock".
• the Figure depicts one possible embodiment of the instant invention.
• Catalyst or catalyst precursor is mixed with the feedstream to be processed.
• the feedstream and catalyst/precursor then enter the solvent deasphalting unit and are treated under solvent deasphalting conditions to produce a catalyst-containing asphalt stream and a deasphalted oil.
• the deasphalted oil may then go through a flash step to recover solvent which is recycled back to the deasphalting unit.
• the catalyst-containing asphalt stream is passed to a slurry hydroprocessing (SHP) unit where it is treated under SHP conditions and then subsequently to a separation zone (e.g., solvent deasphalting or vacuum distillation) to recover hydroconverted product and unconverted asphaltic residue.
• SHP slurry hydroprocessing
• separation zone e.g., solvent deasphalting or vacuum distillation
• a feed is processed utilizing a once-through process to cleave valuable, refinable hydrocarbon groups (saturates, naphthenoaromatics, alkylaromatics, etc.) from large polynuclear aromatic molecules that comprise the asphaltic components of heavy feeds.
• the process includes solvent deasphalting followed by slurry hydrotreating.
• catalyst concentration on feed needed to suppress the formation of coke precursors during the hydroprocessing step is less when using the asphaltic fraction of a given crude than when using the whole crude.
• catalyst or catalyst precursor is mixed with whole crude or with a residual fraction thereof.
• the mixture then enters a solvent deasphalter where the feed is separated into a deasphalted oil and a catalyst-containing asphalt stream.
• the asphalt stream is then fed to a slurry hydroprocessing reactor.
• feeds which may be treated in accordance with the teachings herein are heavy feeds (virgin crudes) and petroleum distillation residues having an API gravity of ⁇ 10 to 15° with a viscosity of > 60 centistokes at 60°C.
• the feeds which enter the solvent deasphalter of step (a) are virgin feeds or crudes which have not yet been hydroprocessed.
• the feeds are unhydroprocessed or non-hydroprocessed feeds.
• This allows for the initial solvent deasphalting (SDA) to recover as much valuable, virgin solvent deasphalted oil as possible and the subsequent hydroprocessing step to operate only on the most refractory (asphalt) fraction to remove aliphatic/naphthenic groups from the aromatic cores.
• the feed to the hydroprocessing step (b) consist essentially of, or consist of, the asphalt product from a solvent deasphalted feed.
• the solvent deasphalter is operated using a C3, C4, C5 paraffin or natural gas condensate, or combinations thereof, at about 275 to about 310°F at appropriate pressures and times to allow a separation to take place and equilibrium to be achieved thereby allowing for recovery of a deasphalted oil product (DAO) and an asphalt product. Pressures and times are easily determined by the skilled artisan.
• the slurry hydroprocessing (SHP) process, or hydroprocessing step can be run using a typical SHP catalyst or precursor such as vanadyl oxylate or phosphomolybdic acid.
• catalyst precursor means a catalytically active material which need only undergo activation/sulfiding to function catalytically.
• Catalysts can be made in several ways including in-situ decomposition of a soluble or dispersible inorganic or organic molybdenum compound in oil. See, for example, U.S. 4,134,825; U.S. 4,548,700; U.S. 4,740,489; and U.S. 5,039,392.
• the asphalt product from solvent deasphalting which contains metals native to the feed being treated, can be calcined in a controlled manner to provide a metals- rich ash that can be utilized as catalyst for the hydroprocessing step.
• catalyst derived from the asphalt product from solvent deasphalting it is fed to a calciner and calcined at temperatures of less than about 1200°F to avoid sintering.
• the burn is conducted below 1100°F and, more preferably, below 1000°F.
• a minimum temperature of about 570°F will be used for calcination.
• Controlled calcination produces a finely divided metals-rich ash which is utilized as catalyst for a SHP process.
• the asphalt can be passed to a coker prior to the controlled calcination step to obtain liquid products boiling below about 950°F, gaseous products, and a coke product which is then fed to the calciner to obtain the metals-rich ash.
• General process conditions for SHP include temperatures of about 650° to about 850°F and pressures from about 800 to about 2500 psig for reactor holding times sufficient to attain about 1025+°F to 1025-°F conversion of at least about 30%, preferably about 40%, and most preferably from about 50% to 60% or above.
• Catalyst concentration on feed required for slurry hydroprocessing depends on the metal (or combination of metals) chosen, as well as on particle size of the catalyst composite. Above all, a sufficient amount of catalyst must be used to suppress the formation of incompatible carbonaceous material (toluene insoluble coke), such that the yield of this material is no more than 0.5 wt% based on feed, preferably less than 0.4 wt% and most preferably below 0.1 wt% so as to avoid reactor fouling.
• Conditions for solvent deasphalting of the SHP product oil will depend on the quality of product desired and are well known to those skilled in the art. However, in a preferred process mode, conditions are chosen such that the yield of upgraded, essentially asphaltene-free product (upgraded oil of step (c)) that is recovered from the asphalt feed will range from about 50 to 70 wt%. Generally, the highest yield is obtained when solvent deasphalting is used to recover upgraded liquid as compared to recovery via distillation. As used herein, essentially asphaltene-free means that the product contains only trace amounts of asphaltene remaining following the SHP process.
• Liquid conversion product from the SHP reactor can be recovered by vacuum flash distillation or by solvent deasphalting (SDA). If SDA is chosen, the SHP product may be sent to the solvent deasphalter that is used for the process feed. In such an integrated operation, a portion of the asphalt from solvent deasphalting that is sent to the SHP unit will be purged to control buildup of catalyst solids and nonconvertible asphalt fractions. In such a process, a means of catalyst recycle is also provided. Alternatively, a small dedicated deasphalter could be used to recover SHP product.
• the recovered SHP product i.e., the essentially asphaltene-free liquid product, may be combined with the DAO from the initial SDA step to provide a finished upgraded crude. Unconverted asphalt (recovered by distillation as an asphalt rich bottoms, or as the asphalt purge stream from solvent deasphalting) may be used as fuel, or feed to a coker or partial oxidation unit.
• a second solvent deasphalting step will be used.
• an integrated process could be run whereby the initial solvent deasphalting (a) is conducted, the asphalt is then passed to the hydrotreater (b), and the liquid conversion product from the hydrotreater is recycled to the solvent deasphalter (c).
• step (a) or step (c) can be used to provide catalyst for the hydrotreater affording a fully integrated process.
• purge of built up catalyst would be required and a sufficient amount of ash catalyst to fuel the hydroprocessing step would be produced.
• the yield and quality of the upgraded crudes produced herein is dependent upon the conditions selected for the feed deasphalting unit (DAU). For example, the yield of upgraded crude (virgin DAO plus 1025-°F liquid from hydroprocessing) increases from 83% to 89% when butane is substituted for propane in the feed deasphalting step (Table 2). With pentane, deasphalting yields should exceed 90 vol%.
• DAU feed deasphalting unit
• Reference to Test No. E illustrates the yield and quality credits inherent in the present invention relative to what can be obtained by deasphalting alone (Table 1, C4 deasphalting column). Note that overall liquid yield has increased from 70.0 wt% on bitumen (for deasphalting alone ) to 85% for the combination process. Moreover, liquid quality (metals, Conradson Carbon) is superior for the combination process product.
• the product resulting from the hydroprocessing of C 3 asphaltenes under the conditions described in Table 2 using 50 ppm of catalyst was deasphalted with a 7:1 volume of C 5 (pentane) solvent.
• the precipitated asphaltenes were removed by filtration and the C5 solvent was removed by evaporation.
• This DAO sample was blended in the appropriate ratio with the light fraction collected during the hydroprocessing experiment and also the appropriate ratio of the C3 DAO.
• the overall liquid yield of the process is 85.8 weight percent.
• the density of the blended product is 0.9343 at 15°C, sulfur is 3.26 wt% and the viscosity is 71 cP at 25°C.

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• Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Engineering & Computer Science (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Working-Up Tar And Pitch (AREA)

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• 2001
  • 2001-02-13 CA CA002398252A patent/CA2398252A1/en not_active Abandoned
  • 2001-02-13 JP JP2001560324A patent/JP2003523451A/ja active Pending
  • 2001-02-13 AU AU2001238235A patent/AU2001238235A1/en not_active Abandoned
  • 2001-02-13 EP EP01910647A patent/EP1268713A1/en not_active Withdrawn
  • 2001-02-13 CN CN 01805006 patent/CN1400997A/zh active Pending
  • 2001-02-13 WO PCT/US2001/004675 patent/WO2001060952A1/en not_active Application Discontinuation

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