EP2227518A2 - Hydrocraquage à hydrogénation ciblée - Google Patents

Hydrocraquage à hydrogénation ciblée

Info

Publication number
EP2227518A2
EP2227518A2 EP08867887A EP08867887A EP2227518A2 EP 2227518 A2 EP2227518 A2 EP 2227518A2 EP 08867887 A EP08867887 A EP 08867887A EP 08867887 A EP08867887 A EP 08867887A EP 2227518 A2 EP2227518 A2 EP 2227518A2
Authority
EP
European Patent Office
Prior art keywords
range
feed
hydroprocessing
stream
hydrogen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP08867887A
Other languages
German (de)
English (en)
Inventor
Subhasis Bhattacharya
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Chevron USA Inc
Original Assignee
Chevron USA Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Chevron USA Inc filed Critical Chevron USA Inc
Publication of EP2227518A2 publication Critical patent/EP2227518A2/fr
Withdrawn legal-status Critical Current

Links

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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/043—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by fractional condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • 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
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • 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
    • 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
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural parallel stages only
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/307—Cetane number, cetane index
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • This invention is directed to a partial conversion hydrocracking (HCR) unit, in which unconverted oil is fed to a Fluid Catalytic Cracking (FCC) unit.
  • HCR partial conversion hydrocracking
  • FCC Fluid Catalytic Cracking
  • vacuum gas oil hydrotreaters and hydrocrackers are employed to remove impurities such as sulfur, nitrogen and metals from the feed.
  • the middle distillate boiling material (boiling in the range from 250 ° F -735T ) from VGO hydrotreating or moderate severity hydrocrackers does not meet the smoke point, the cetane number or the aromatic specification required
  • Hydroprocessing technology (which encompasses hydrotreating, hydrocracking and hydrodewaxing processes) aims to increase the value of the crude oil by fundamentally rearranging molecules The end products are also made more environmentally friendly.
  • this middle distillate is separately upgraded by a middle distillate hydrotreater or, alternatively, the middle distillate is blended into the general fuel oil pool or used as home heating oil
  • hydroprocessing schemes have been developed which permit the middle distillate to be hydrotreated in the same high pressure loop as the vacuum gas oil hydrotreating reactor or the moderate severity hydrocracking reactor. The investment cost saving and/or utilities saving are significant since a separate middle distillate hydrotreater is not required.
  • U.S. Pat. No. 6,787,025 also discloses multi-stage hydroprocessing for the production of middle distillates.
  • a major benefit of this invention is the potential for simultaneously upgrading difficult cracked stocks such as Light Cycle Oil, Light Coker Gas Oil and Visbroken Gas Oil or Straight-Run Atmospheric Gas Oils utilizing the high-pressure environment required for mild hydrocracking.
  • U.S. Pat. No. 7,238,277 provides very high to total conversion of heavy oils to products in a single high-pressure loop, using multiple reaction stages.
  • the second stage or subsequent stages may be a combination of co-current and counter-current operation.
  • the benefits of this invention include conversion of feed to useful products at reduced operating pressures using lower catalyst volumes. Lower hydrogen consumption also results. A minimal amount of equipment is employed. Utility consumption is also minimized.
  • U.S. Publication 20050103682 relates to a multi-stage process for hydroprocessing gas oils.
  • each stage possesses at least one hydrocracking zone.
  • the second stage and any subsequent stages possess an environment having a low heteroatom content.
  • Light products such as naphtha, kerosene and diesel, may be recycled from fractionation (along with light products from other sources) to the second stage (or a subsequent stage) in order to produce a larger yield of lighter products, such as gas and naphtha.
  • Pressure in the zone or zones subsequent to the initial zone is from 500 to 1000 psig lower than the pressure in the initial zone, in order to provide cost savings and minimize overcracking.
  • a method for hydroprocessing a hydrocarbon feedstock employing multiple hydroprocessing zones within a single reaction loop, each zone having one or more catalyst beds, comprising the following steps:
  • step (a) passing a hydrocarbonaceous feedstock to a first hydroprocessing zone having one or more beds containing hydroprocessing catalyst, the hydroprocessing zone being maintained at hydroprocessing conditions, wherein the feedstock is contacted with catalyst and hydrogen; (b) passing the effluent of step (a) directly to a hot high pressure separator, wherein the effluent is separated to produce a vapor stream comprising hydrogen, hydrocarbonaceous compounds boiling at a temperature below the boiling range of the hydrocarbonaceous feedstock, hydrogen sulfide and ammonia and a liquid stream comprising hydrocarbonaceous compounds boiling approximately in the range of said hydrocarbonaceous feedstock;
  • step (c) passing the vapor stream of step (b) after cooling and partial condensation, to a hot high pressure separator where it is flashed, thereby producing an overhead vapor stream and a liquid stream, wherein the liquid stream, which comprises hydrotreated hydrocarbons in the middle distillate range, is passed to a second hydroprocessing zone;
  • step (d) passing the overhead vapor stream from the hot high pressure separator of step (c), after cooling and contact with water, said vapor stream comprising hydrogen, ammonia, hydrogen sulfide, light gases and naphtha, to a cold high pressure separator, where hydrogen, hydrogen sulfide, and light hydrocarbonaceous gases are removed overhead, ammonia is removed from the cold high pressure separator as ammonium bisulfide in the sour water stripper, and naphtha and middle distillates are passed to fractionation
  • step (e) passing the liquid stream from the hot high pressure separator of step (b) to a hot low pressure separator, where it is flashed to produce an overhead stream comprising gases and a liquid stream comprising unconverted oil;
  • step (f) passing the liquid stream of step (e) which comprises unconverted oil, to a steam stripper, where lighter material is removed overhead as a vapor stream, and a liquid stream, which comprises stripped unconverted oil, is recovered.
  • the Figure illustrates the flow scheme of the current invention.
  • feedstocks include any heavy or synthetic oil fraction or process stream having a boiling point above 392 ° F. (200 ° C).
  • feedstocks include vacuum gas oils (VGO), heavy coker gas oil (HCGO), heavy atmospheric gas oil (AGO), light coker gas oil (LCGO), visbreaker gas oil (VBGO), demetallized oils (DMO), vacuum residua, atmospheric residua, deasphalted oil (DAO), Fischer-Tropsch streams, Light Cycle Oil, Light Cycle Gas Oil and other FCC product streams.
  • a middle distillate fraction is defined as having an approximate boiling range from about 250 to 700 ° F. At least 75 vol.%, preferably 85 vol.% of the components of the middle distillate have a normal boiling point of greater than 250 ° F. At least about 75 vol.%, preferably 85 vol.% of the components of the middle distillate have a normal boiling point of less than 700 ° F.
  • the term "middle distillate” includes the diesel, jet fuel and kerosene boiling range fractions. The kerosene or jet fuel boiling point range refers to the range between 280 and 525 ° F (138-274O).
  • diesel boiling range refers to hydrocarbons boiling in the range from 250 to 700T (121 -371 ° C).
  • Gasoline or naphtha may also be produced in the process of this invention. Gasoline or naphtha normally boils in the range below 400T. (204 ° C), or C 5 to 400T. Boiling ranges of various product fractions recovered in any particular refinery will vary with such factors as the characteristics of the crude oil source, local refinery markets and product prices.
  • Hydroprocessing conditions is a general term which refers primarily in this application to hydrocracking or hydrotreating.
  • Hydrotreating conditions include a reaction temperature between 400T.-950T. (204O.-482O.), preferably 600T.-850T. (315 ° C-464 ° C); a pressure between 500 to 5000 psig (pounds per square inch gauge) (3.5-34.6 MPa), preferably 1000 to 3000 psig (7.0-20.8 MPa): a feed rate (LHSV) of 0.3 hr-1 to 20 hr-1 (v/v) preferably from 0.5 to 4.0; and overall hydrogen consumption 300 to 2000 SCF per barrel of liquid hydrocarbon feed (63.4-356 m 3 /m 3 feed).
  • a reaction temperature between 400T.-950T. (204O.-482O.), preferably 600T.-850T. (315 ° C-464 ° C); a pressure between 500 to 5000 psig (pounds per square inch gauge) (3.5-34.6 MPa), preferably 1000 to 3000 psig (7.0-20.8 MPa): a feed rate (LHSV) of 0.3 h
  • Typical hydrocracking conditions include a reaction temperature of from 400T.-950T. (204O.-510 ° C.), preferably 650T.-850T. (315 ° C.-454 ° C).
  • Reaction pressure ranges from 500 to 5000 psig (3.5-4.5 MPa), preferably 1000-3000 psig (7.0-20.8 MPa).
  • LHSV ranges from 0.1 to 15 hr-1 (v/v), preferably 0.5 to 5.0 hr-1.
  • Hydrogen consumption ranges from 500 to 2500 SCF per barrel of liquid hydrocarbon feed (89.1-445 m 3 H 2 /m 3 feed).
  • Catalyst A hydroprocessing zone may contain only one catalyst, or several catalysts in combination.
  • the hydrocracking catalyst generally comprises a cracking component, a hydrogenation component and a binder.
  • the cracking component may include an amorphous silica/alumina phase and/or a zeolite, such as a Y-type or USY zeolite. Catalysts having high cracking activity often employ REX, REY and USY zeolites.
  • the binder is generally silica or alumina.
  • the hydrogenation component will be a Group Vl, Group VII, or Group VIII metal or oxides or sulfides thereof, preferably one or more of molybdenum, tungsten, cobalt, or nickel, or the sulfides or oxides thereof.
  • these hydrogenation components generally make up from about 5% to about 40% by weight of the catalyst.
  • platinum group metals especially platinum and/or palladium, may be present as the hydrogenation component, either alone or in combination with the base metal hydrogenation components molybdenum, tungsten, cobalt, or nickel. If present, the platinum group metals will generally make up from about 0.1% to about 2% by weight of the catalyst.
  • Hydrotreating catalyst is typically a composite of a Group Vl metal or compound thereof, and a Group VIII metal or compound thereof supported on a porous refractory base such as alumina.
  • Examples of hydrotreating catalysts are alumina supported cobalt-molybdenum, nickel sulfide, nickel- tungsten, cobalt-tungsten and nickel-molybdenum.
  • such hydrotreating catalysts are presulfided.
  • high activity hydrotreating catalyst suitable for high levels of hydrogenation.
  • Such catalysts have high surface areas (greater than 140 m.sup.2 /gm) and high densities (0.7-0.95 gm/cc).
  • the high surface area increases reaction rates due to generally increased dispersion of the active components.
  • Higher density catalysts allow one to load a larger amount of active metals and promoter per reactor volume, a factor which is commercially important. Since deposits of coke are thought to cause the majority of the catalyst deactivation, the catalyst pore volume should be maintained at a modest level (0.4-0.6).
  • a high activity catalyst is at times desired in order to reduce the required operating temperatures. High temperatures lead to increased coking.
  • the hydrotreated reactor effluent exchanges heat in exchanger 5 with the reactor feed (stream 2 prior to entering the exchanger 5 and stream 9 upon leaving the exchanger 5).
  • Stream 12 is flashed in hot high pressure separator 40 at high temperature and pressure conditions to recover most of the unconverted oil (UCO) components in the liquid phase (stream 13). Vapor leaves separator 40 overhead in line 22, and heat is exchanged with hydrogen stream 31 in exchanger 25.
  • Stream 22 is finally cooled to about 200°C in the hot high pressure separator vapor/recycle gas exchanger 25.
  • Stream 22 is then flashed in hot high pressure separator 50.
  • hot high pressure separator 50 At these relatively high pressure and low temperature conditions, most of the hydrotreated jet and diesel range material is recovered as liquid stream 27 at high pressure, which is pumped(pump 35) to the feedstream (stream 11 ) , which passes to hydrocracking reactor 20, for further processing.
  • the overhead vapor from the hot high pressure separator 50, stream 23, is then cooled in an air cooler (not shown) before entering a cold high pressure separator (not shown).
  • the overhead vapor stream, stream 23, comprises hydrogen, ammonia, and hydrogen sulfide, along with light gases and naphtha.
  • Stream 13 passes to hot low pressure separator 60, where it is flashed. Vapor is removed as stream 28. The hot low pressure separator bottoms are removed as stream 73 and passed to UCO (unconverted oil) stripper 30. The material of stream 73 is stream stripped in stripper 30 to recover any lighter material in the UCO stream. Lighter material is removed as stream 26. Jet and diesel range material is withdrawn as a side draw 17 from the column. Side draw 17 combines with stream 19, stripper bottoms 16 (UCO) to become stream 19. A side stream 18 may be taken from bottoms stream 16. Stream 19, recycle oil, is pumped, via pump 45, to storage drum 70. The recycle oil exits storage drum 70 through stream 21 and is pumped, by means of pump 55, to stream 11. Stream 11 is heated in exchanger 15 prior to entering hydrocracking reactor 20 for further aromatic saturation. The overhead liquid stream 26 from the UCO stripper 30 is sent to the main product stripper, and the offgas is sent to fuel gas (not shown).
  • UCO unconverted oil
  • the hydrotreated, stripped UCO (stream 16) from the bottom of the UCO stripper is an excellent quality FCC feed.
  • a part of stripped unconverted oil (stream 18) is sent out as FCC feed. Further saturation of the FCC feed is thus avoided.
  • Only a limited portion of the UCO (mixed with stream 19, is passed to hydrocracker 20 for further saturation of aromatic components and conversion to distillate products. The amount recycled back is based on the desired overall conversion level.
  • the second stage hydrocracking reactor 20 is loaded with hydrocracking catalyst and operates under a clean environment (no heteroatoms), ideally selectively converting the UCO to desired products and further saturating the aromatic components to achieve required jet and diesel properties at different conversion levels.
  • Stream 32 is a sidestream from stream 1. From stream 32, streams 7 and 8 add hydrogen in between the first and second beds and second and third beds of reactor 20 respectively. 1 Both the hydrotreating reactor 10 and hydrocracking reactor 20 are designed
  • hydrocracking unit The table indicates that there is no need in

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

Abstract

L'invention porte sur un processus de traitement dans lequel une unité d'hydrocraquage (HCR) à conversion partielle, précédée de préférence d'une unité d'hydrotraitement, alimente une unité de craquage catalytique fluide (FCC) en huile non transformée. La plupart des raffineries exploitent l'unité FCC à sa pleine capacité afin d'arriver à une utilisation optimale des ressources. Lors de l'arrêt des unités de désulfuration de résidus alimentant l'unité FCC, il est souhaitable de réduire la conversion dans l'hydrocraqueur qui alimente l'unité FCC afin de maximiser l'alimentation de ladit unité. Il est possible de produire des carburants aviation et diesel conformes aux normes lorsque l'unité HCR fonctionne avec un faible taux de conversion. Cela permet en outre d'éviter une sursaturation indésirable de l'huile non transformée (UCO) en provenance de l'unité HCR qui alimente l'unité FCC, et de prévenir toute consommation excessive d'hydrogène. La saturation aromatique additionnelle des produits de distillat intermédiaires en provenance de l'unité HCR à faible taux de convesrion s'effectue normalement dans une unité de post-traitement séparée.
EP08867887A 2007-12-21 2008-12-15 Hydrocraquage à hydrogénation ciblée Withdrawn EP2227518A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US12/004,751 US20090159493A1 (en) 2007-12-21 2007-12-21 Targeted hydrogenation hydrocracking
PCT/US2008/086831 WO2009085696A2 (fr) 2007-12-21 2008-12-15 Hydrocraquage à hydrogénation ciblée

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EP2227518A2 true EP2227518A2 (fr) 2010-09-15

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EP08867887A Withdrawn EP2227518A2 (fr) 2007-12-21 2008-12-15 Hydrocraquage à hydrogénation ciblée

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US (1) US20090159493A1 (fr)
EP (1) EP2227518A2 (fr)
JP (1) JP2011508018A (fr)
AR (1) AR071549A1 (fr)
AU (1) AU2008343372A1 (fr)
CA (1) CA2709361A1 (fr)
TW (1) TW200940697A (fr)
WO (1) WO2009085696A2 (fr)
ZA (1) ZA201004297B (fr)

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AU2008343372A1 (en) 2009-07-09
WO2009085696A3 (fr) 2010-01-21
ZA201004297B (en) 2011-08-31
CA2709361A1 (fr) 2009-07-09
JP2011508018A (ja) 2011-03-10
WO2009085696A2 (fr) 2009-07-09
TW200940697A (en) 2009-10-01
AR071549A1 (es) 2010-06-30
US20090159493A1 (en) 2009-06-25

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