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
  • C10G67/06—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 a sorption process as the refining step in the absence of hydrogen
• • 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

Definitions

• the present invention relates to a process for heteroatom removal from a petroleum and/or chemical stream.
• the present invention is particularly useful in the process of ensuring the desired product quality by enabling the heteroatom removal process to continue in the event of a process excursion.
• Heteroatom removal is one of the fundamental processes of the refining and petrochemical industries. Heteroatoms are defined to be those atoms other than hydrogen and carbon, present in hydrocarbon streams, including but not limited to, sulfur, nitrogen, oxygen, and halogens. These atoms are typically found as organo heteroatom molecules wherein the heteroatoms molecules make-up part of the carbon hydrogen backbone. Unless otherwise specified, the expression "heteroatom” is hereafter meant to encompass the elemental form of the heteroatom itself as well as its combined counterpart species as an organic and as combined with hydrogen (i.e. organo heteroatom and hetero-hydride, respectively).
• hetero- hydride i.e. hydrogen sulfide, ammonia, water, or hydrogen halide
• hydroprocessing catalyst which is designed to meet the required product quality specifications, or to supply a low or a substantially reduced level (hereafter low is meant to also include essentially no heteroatoms) heteroatom stream to subsequent heteroatom sensitive processes, catalysts, or product dispositions.
• catalytic heteroatom removal of a stream is carried out in co-current reactors in which both the preheated feed stream and a hydrogen-containing treat gas are introduced to one or more beds of heteroatom removal catalyst.
• the liquid feed stock, any vaporized hydrocarbons, and hydrogen-containing treat gas all flow together through the catalyst bed(s).
• the resulting combined vapor phase and liquid phase effluents are normally separated in a series of one or more separator vessels, or drums, downstream of the reactor.
• Process excursions can occur during operation of a co-current reactor.
• Process excursions include events such as variation in quality or rate of the liquid feed stream or hydrogen containing treat gas stream, start-up and shut- down of the unit, emergency depressuring of the reactor to avert hazardous conditions, or other process upsets commonly experienced by commercial operating units.
• events such as variation in quality or rate of the liquid feed stream or hydrogen containing treat gas stream, start-up and shut- down of the unit, emergency depressuring of the reactor to avert hazardous conditions, or other process upsets commonly experienced by commercial operating units.
• process excursions there is a high probability that the heteroatom removal capability of the co-current reactor will be diminished and either the heteroatoms in their original form as organo heteroatom molecules or as the hetero-hydride will come in contact with the heteroatom sensitive downstream process or catalyst. Such contact may cause temporary or permanent impairment of the sensitive process or catalyst and result in unacceptable final product quality which may require significant time and expense (i.e., replacement of a poisoned catalyst) to rectify.
• a bed of heteroatom sorbent can be used to protect downstream processes or catalyst but, if a bed of heteroatom sorbent is used downstream of a co- current heteroatom removal zone in co-current operation, a separation step for removal of the hetero-hydride is required.
• the sorbents bed's capacity can be quickly diminished if substantial heteroatom breakthrough of the upstream heteroatom hydroprocessing catalyst occurs and restoration of capacity will typically require off stream regeneration.
• heteroatom removal can be accomplished more efficiently in a countercurrent flow hydroprocessing system wherein a hydroprocessing catalyst system through which the liquid hydrocarbon feedstream flows downward and the hydrogen containing treat gas is passed upward.
• the counter current flow system has the potential to produce significantly lower heteroatom content streams and to do so more efficiently.
• US-A-3, 147,210 discloses a two stage process for the hydrofining-hydrogenation of high-boiling range aromatic hydrocarbons.
• the feed stock is first subjected to catalytic hydrofining, preferably in co-current flow with hydrogen, then subjected to hydrogenation over a heteroatom sensitive noble metal hydrogenation catalyst countercurrent to the flow of a hydrogen containing treat gas.
• US-A-3,767,562 and US-A-3,775,291 disclose a countercurrent process for producing jet fuels, whereas the jet fuel is first hydrodesulfurized in a co-current mode prior to two stage countercurrent hydrogenation.
• US-A-5, 183,556 also discloses a two stage co-current/countercurrent process for hydrofining and hydrogenating aromatics in a diesel fuel stream.
• the heteroatom removal process of the present invention is applicable to all heteroatom bearing compounds common to petroleum and chemical streams, the process is particularly suitable for the removal of the least reactive, most highly refractory heteroatom species.
• the process of the present invention can result in a product stream which contains essentially no heteroatoms.
• the phrase "essentially no heteroatoms" depends upon the overall process being considered, but can be defined as a value substantially less than about 100 wppm, preferably less than about 10 wppm, more preferably less than about 1 wppm, and most preferably less than about 0.1 wppm as measured by existing, conventional analytical technology.
• the invention is also applicable to consistent production of low heteroatom content streams.
• the feed stocks of the present invention are subjected to heteroatom removal in at least one catalyst bed, or reaction zone, wherein feed stock flows co- current or countercurrent to the flow of a hydrogen-containing treat gas.
• Each zone may be immediately preceded and followed by a non-reaction zone where products may be removed and/or feed or treat gas introduced.
• the non-reaction zone will be a zone which is typically empty and does not contain a catalyst that is capable of removing any heteroatoms, but it could contain a drying agent, such as a molecular sieve bed. In a preferred embodiment, such a non-reaction zone is an empty cross-section in the reaction vessel.
• the liquid effluent from the reaction zone(s), is passed on to at least one sorbent zone containing one or more heteroatom sorbents in contact with a countercurrent flow of hydrogen containing treat gas.
• the liquid effluent, now with reduced low heteroatom content, wherein the initial level of heteroatom in the hydrocarbon feedstream is reduced by levels in the range of from about 20% to about 100%, may be sent to a heteroatom sensitive process, catalyst, or product disposition.
• the liquid effluent contains a heteroatom content which has been reduced by levels in the range from about 50% to about 100%, more preferably from about 75% to about 100%, and most preferably from about 90% to about 100%.
• the heteroatom sensitive process may be discrete from the countercurrent system, but is preferentially operated in countercurrent mode and may be contained within the same vessel.
• the hydrocarbon feed steam first passes through a co- current hydrotreating reaction zone which contains one or more hydroprocessing catalyst(s).
• the effluent may then be passed to at least one countercurrent reaction zone containing a stacked catalyst/sorbent bed system.
• the heteroatom hydroprocessing catalyst will convert essentially all of the organo heteroatom molecules to the corresponding hetero-hydride.
• the hetero-hydride partitions into the vapor phase due to its inherent vapor pressure under hydroprocessing conditions and is carried upward by the up flowing hydrogen-containing treat gas.
• the sorbent zone sees a negligible amount of heteroatom so that its capacity is not consumed.
• a process upset where unreacted organo heteroatom molecules or the hetero-hydride reaction products break through the catalyst zone they will be sorbed by the heteroatom sorbent material thereby protecting the downstream heteroatom sensitive process or catalyst.
• the sorbent may irreversibly bind with the sorbent which, while protecting the down stream process or catalyst, will result in the sorbent needing to be replaced or regenerated at some frequency. It is preferred that the sorbent material also catalyze or otherwise facilitate the reaction of hydrogen with the sorbed organo heteroatom molecules to form the corresponding hetero- hydride.
• the hetero-hydride is typically more weakly bound by the sorbent and due to its inherent high vapor pressure can be stripped from the sorbent zone by the up flowing treat gas thereby continuously regenerating the sorbent bed.
• a third way that the sorbent bed can function is to reversibly bind with the heteroatom and slowly release it to the down stream process or catalyst.
• This third type of sorption system may also be enhanced by a small zone of heteroatom hydroprocessing catalyst placed below the sorbent bed and operated in contact with a countercurrent flow of hydrogen containing treat gas. The said additional catalyst zone will convert the organo heteroatom molecules to the corresponding hetero-hydride and allow them to be stripped from the system by the up flowing treat gas.
• reaction zones and sorption zones can either be in the same vessel separated by non-reaction zones, or any can be in separate vessels.
• the non-reaction zones in the later case will typically be the transfer lines leading from one vessel to another.
• the said low heteroatom streams can be passed on to other catalysts or processes which are extremely sensitive to poisoning by heteroatoms. This heteroatom sensitivity is sometimes sufficiently acute as to prevent the practical use of advanced catalysts.
• Such catalysts include those which promote ring opening, aromatic saturation, isomerization, and hydrocracking.
• a preprocessing step is performed to remove the so-called “easy heteroatoms"
• the vapor and liquid are disengaged and the liquid effluent directed to the top of a countercurrent reactor.
• the vapor from the preprocessing step can be processed separately or combined with the vapor phase product from the countercurrent reactor.
• the vapor phase product(s) may undergo further vapor phase hydroprocessing if greater reduction in heteroatom and aromatic species is desired or sent directly to a recovery system.
• the catalyst may be contained in one or more beds in one vessel or multiple vessels.
• Various hardware i.e. distributors, baffles, heat transfer devices
• Suitable heteroatom hydroprocessing catalyst for use in the upstream countercurrent zone(s) or co-current reaction zone(s) can be any conventional hydroprocessing catalyst and includes hydrotreating catalysts, hydrocracking catalysts, and hydrogenation catalysts; one or more may be used in either zone depending on the starting quality of the feed and the desired product quality. Most common are those which comprise at least one Group VIII metal, preferably Fe, Co and Ni, more preferably Co and/or Ni, and most preferably Ni; and at least one Group VI metal, preferably Mo and W, on a high surface area support material, which preferably is zeolite or alumina.
• Catalysts suitable for said portions are those comprised of a noble or non-noble metal, or metals, of Group VIII of the Periodic Table of the Elements supported in a highly dispersed and essentially uniformly distributed manner on a refractory inorganic support.
• Suitable support materials for the catalysts of the present invention include high surface area, refractory materials, such as alumina, silica, aluminosilicates, silicon carbide, amorphous and crystalline silica-aluminas, silica magnesias, boria, titania, zirconia and the like.
• the preferred support materials include alumina and the crystalline silica- aluminas, particularly those materials classified as clays or zeolites, more preferably controlled acidity zeolites modified by their manner of synthesis, by the incorporation of acidity moderators, and post-synthesis modifications such as dealumination.
• Heteroatom sorbents suitable for use in the practice of the present invention include those selected from several classes of materials known to be reactive toward the organo heteroatom molecules and in some cases the hetero- hydride and capable of binding same in either a reversible or irreversible manner.
• One class of materials suitable for such use as heteroatom sorbents are reduced metals which may be employed as bulk materials or supported on an appropriate support material such as an alumina, silica, or a zeolite.
• Representative metals include those from Groups la, lb, lla, lib, IIIA, IVA, VB, VIB, VIIB, VIII or the Periodic Table of the Elements (as displayed inside the front cover of the 64 th Edition of the CRC Handbook of Chemistry and Physics).
• Preferred metals include Zn, Fe, Ni, Cu, Mo, Co, Mg, Mn, W, K, Na, Ca, Ba, La, Ce, V, Ta, Nb, Re, Zr, Cr, Ag, Rh, lr, Pd, Pt, and Sn. These metals may be employed individually or in combination.
• metal oxides which may be employed as bulk oxides or supported on an appropriate support material such as an alumina, silica, or a zeolite.
• Representative metal oxides include those of the metals from Groups la, lb, lla, lib, IIIA, IVA, VB, VIB, VIIB, VIII or the Periodic Table of the Elements.
• Preferred metals include Zn, Fe, Ni, Cu, Mo, Co, Mg, Mn, W, K, Na, Ca, Ba, La, Ce, V, Ta, Nb, Re, Zr, Cr, Ag, Rh, lr, Pd, Pt, and Sn. These metal oxides may be employed individually or in combination.
• a third class of metal based materials suitable for such use as heteroatom sorbents are metal sulfides which may be employed as bulk sulfides or supported on an appropriate support material such as an alumina, silica, or a zeolite.
• Representative metal oxides include those of the metals from Groups la, lb, lla, lib, IIIA, IVA, VB, VIB, VIIB, VIII or the Periodic Table of the Elements.
• Preferred metals include Zn, Fe, Ni, Cu, Mo, Co, Mg, Mn, W, K, Na, Ca, Ba, La, Ce, V, Ta, Nb, Re, Zr, Cr, Ag, Rh, lr, Pd, Pt, and Sn. These metal sulfides may be employed individually or in combination.
• Zeolites and zeolite based materials may serve as heteroatom sorbents for this invention as detailed in US-A-4,831,206 and US-A-4, 831 ,207, both of which are also incorporated herein by reference. These materials share with spinels the ability to function as regenerable heteroatom sorbents and permit operation of this invention in a mode cycling between heteroatom capture and heteroatom release in either continuous or batch operation depending upon the process configuration. Zeolites incorporating heteroatom active metals by ion exchange are also of value to this invention.
• Examples include Zn4A, chabazite, and faujasite moderated by the incorporation of zinc phosphate, and transition metal framework substituted zeolites similar to, but not limited to, US-A- 5,185,135 and US-A-5,283,047, both of which are also incorporated herein by reference.
• Spinels represent another class of heteroatom sorbents suitable for use in the practice of the present invention. Such materials are readily synthesized from the appropriate metal salt, frequently a sulfate, and sodium aluminate under the influence of a third agent like sulfuric acid.
• hydrotalcite exhibit high heteroatom capacities and for this reason serve as heteroatom sorbents for this invention.
• These may include numerous modified and unmodified synthetic and mineral analogs of these as described in US-A-3,539,306; US-A-3,796,792; US-A-3,879,523; and US-A-4,454,244, all of which are also incorporated herein by reference.
• the high molecular dispersions of the reactive metal make them very effective scavengers for heteroatom bearing molecules.
• activated carbons and acidic activated carbons that have undergone treatment, well known to those skilled in the art, to have an enhanced acidic nature.
• Acidic salts may also be added to the activated carbon, used on other high surface area support or used as bulk sorbents.
• the weight ratio of the heteroatom sorbent to the heteroatom removal catalyst may be in the range of from 0.01 to 10, preferably from 0.05 to 5, and more preferably from 0.1 to 1.
• the sorbent material also catalyzes or otherwise facilitates the reaction of hydrogen with the sorbed organo heteroatom molecules to form the corresponding hetero-hydride.
• the countercurrent contacting of an effluent stream from an upstream reaction zone, with hydrogen-containing treat gas strips dissolved hetero- hydride impurities from the effluent stream, thereby improving both the hydrogen partial pressure and the catalyst performance. That is, the catalyst and sorbent can be on-stream for substantially longer periods of time before regeneration is required. Further, predictable heteroatom removal levels will be achieved by the process of the present invention.
• the process of this invention is operable over a range of conditions consistent with the intended objectives in terms of product quality improvement and consistent with any downstream process with which this invention is combined in either a common or sequential reactor assembly.
• hydrogen is an essential component of the process and may be supplied pure or admixed with other passive or inert gases as is frequently the case in a refining or chemical processing environment. It is preferred that the hydrogen stream be heteroatom free, or essentially heteroatom free, and it is understood that the latter condition may be achieved if desired by conventional technologies currently utilized for this purpose.
• the various embodiments of the present invention include operating conditions consisting of a temperature in the range of from 100 to 500 °C
• Pressures at which the process may operated include those in the range of from 100 to 2000 psig (689 to 13,788 kPa), preferably from 400 to 1200 psig (2758 to 8273 kPa), and more preferably from 450 to 1000 psig (3102 to 6894 kPa).
• Gas rates at which the process may operated include those in the range of from 100 to 10,000 SCF/B (18 to 1781 m 3 gas/m 3 oil), preferably from 250 to 7500 SCF/B (45 to 1336 m 3 gas/m 3 oil), and more preferably from 500 to 5000 SCF/B (89 to 8906 m 3 gas/m 3 oil).
• the feed rate velocity at which the process may be operated varies in the range of from 0.1 to 100 LHSV, preferably from 0.3 to 40 LHSV, and more preferably from 0.5 to 30 LHSV.
• the downstream process, catalyst, of product disposition will require that the liquid stream be at a lower temperature than was required in the heteroatom hydroprocessing steam; particularly when the downstream process/catalyst is performing aromatic saturation that is equilibrium limited at higher temperatures.
• the temperature adjustment prior to contacting the liquid stream with the heteroatom sorbent as most of the sorbents having higher sorption capacities at lower temperatures.
• each of the temperature ranges described above may be decreased by as much as 100 °C (180 °F).
• the hetero-hydrides formed across the heteroatom hydroprocessing catalyst have a finite solubility in the liquid stream. For this reason it may at time be desirable to include a stripping zone to remove these hetero-hydrides before passing the liquid stream to the sorbent zone.
• This stripping zone may be contained within the same vessel or a discrete vessel and may include any type of stripper familiar to those skilled in the art.
• This invention will allow consistent levels of heteroatom concentration in a liquid effluent stream by utilizing a sorbent bed in countercurrent flow operation to sorb higher levels of heteroatoms breaking through the heteroatom hydroprocessing zone during process excursions.

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• 1997
  • 1997-08-22 JP JP10510986A patent/JP2000516663A/ja active Pending
  • 1997-08-22 WO PCT/US1997/014761 patent/WO1998007805A2/en not_active Application Discontinuation
  • 1997-08-22 AU AU43278/97A patent/AU4327897A/en not_active Abandoned
  • 1997-08-22 CA CA002264021A patent/CA2264021A1/en not_active Abandoned
  • 1997-08-22 EP EP97941351A patent/EP0944691A2/de not_active Ceased
• 1999
  • 1999-02-22 NO NO990829A patent/NO990829L/no unknown

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