WO2003104358A1 - Hydrocraqueur a etages multiples avec recyclage de kerosene - Google Patents

Hydrocraqueur a etages multiples avec recyclage de kerosene Download PDF

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Publication number
WO2003104358A1
WO2003104358A1 PCT/US2003/013816 US0313816W WO03104358A1 WO 2003104358 A1 WO2003104358 A1 WO 2003104358A1 US 0313816 W US0313816 W US 0313816W WO 03104358 A1 WO03104358 A1 WO 03104358A1
Authority
WO
WIPO (PCT)
Prior art keywords
hydroprocessing
kerosene
naphtha
zone
range
Prior art date
Application number
PCT/US2003/013816
Other languages
English (en)
Inventor
H. Alex Yoon
Jay Parekh
Arthur J. Dahlberg
Original Assignee
Chevron U.S.A. 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 U.S.A. Inc. filed Critical Chevron U.S.A. Inc.
Priority to EP03726599A priority Critical patent/EP1511824A4/fr
Priority to JP2004511419A priority patent/JP2006510746A/ja
Priority to CA002487381A priority patent/CA2487381A1/fr
Priority to AU2003228827A priority patent/AU2003228827B2/en
Publication of WO2003104358A1 publication Critical patent/WO2003104358A1/fr

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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
    • 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
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking 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

Definitions

  • This invention relates to a multi-stage hydrocracking process in which light products from the first stage, such as naphtha, kerosene and diesel, are joined with naphtha, kerosene and diesel from other sources and recycled from fractionation to a second stage (or subsequent stage) hydrocracker in order to produce lighter products, such as gas and naphtha.
  • first stage such as naphtha, kerosene and diesel
  • second stage or subsequent stage hydrocracker
  • U.S. Pat. No. 4,789,457 discloses a process in which a highly aromatic substantially dealkylated feedstock is processed directly to high octane gasoline by hydrocracking over a catalyst preferably comprising a large pore zeolite such as zeolite Y, in addition to a hydrogenation- dehydrogenation component.
  • the feedstock is preferably a light cycle oil. Light cycle oil is heavier than the kerosene and naphtha cracked in the instant invention, and only one hydrocracking stage is employed in Fischer et al.
  • the invention disclosed herein is a process for the production of light products, such as gas and naphtha, by processing kerosene in a second stage (or a subsequent stage) of a multi-stage hydrocracker. Kerosene, diesel and naphtha from other sources are included in the recycle, and subsequent hydroprocessing stages are maintained at lower pressures than the initial hydroprocessing stage. This results in cost savings.
  • the instant invention is summarized as follows:
  • a method for hydroprocessing a hydrocarbon feedstock employing multiple hydroprocessing zones within a single reaction loop and comprising the following steps:
  • step (b) removing the vapor stream of step (a), which comprises hydrogen, hydrogen sulfide and light hydrocarbonaceous gases overhead;
  • step (c) combining the liquid stream of step (b) with the liquid effluent from other hydroprocessing zones;
  • step (d) passing the liquid stream of step (c), which comprises hydrocarbonaceous compounds boiling in approximately the same range of the hydrocarbonaceous feedstock, to fractionation;
  • step (e) separating the liquid stream of step (d), in fractionation, into gas, naphtha, kerosene and diesel fractions, in addition to the bottoms fraction;
  • step (f) passing the bottoms fraction of step (e) to further processing or recycling to one or more of the other hydroprocessing zones of step (c);
  • step (g) passing one or more of the naphtha, kerosene and diesel fractions to further processing as products or recycling one or more of the fractions to one or more of the other hydroprocessing zones of step (c) the kerosene, naphtha, and diesel fractions being in combination with kerosene, naphtha and diesel fractions from other sources, said hydroprocessing zones or zones being maintained at hydroprocessing conditions and at lower pressure than the first hydroprocessing zone, and possessing an environment substantially free of H 2 S, NH 3 , or other heteroatom contaminants;
  • the Figure illustrates a two-stage hydrocracking process having the capability for recycle of bottoms fractions, diesel fractions, kerosene fraction or naphtha fractions to the second reactor stage.
  • Preheated oil feed in stream 1 is mixed with hydrogen in stream 2 prior to its entrance into first stage or primary hydroprocessing zone 10.
  • This hydroprocessing zone is preferably a downflow, fixed bed reactor.
  • This reactor contains multiple beds of hydroprocessing catalysts. At least one bed contains hydrocracking catalyst.
  • the effluent 3 of the first stage reactor which has been hydrotreated and partially hydrocracked, comprises a liquid stream and a vapor stream.
  • the vapor stream 3(a) is removed overhead. It comprises hydrogen, hydrogen sulfide and light hydrocarbonaceous gases.
  • the liquid stream 3(b) is combined with the liquid effluent from other process zones, represented by stream 4.
  • Stream 3(b) and stream 4 are combined to create stream 5.
  • Stream 5 is passed to the fractionation unit 30, where it is separated into gas stream 6, naphtha stream 7, kerosene stream 8, diesel stream 9, and bottoms stream 14.
  • the naphtha product may alternately be recycled, in whole or in part, through stream 11 to stream 15, and ultimately to second stage reactor 20.
  • Kerosene product may alternately be recycled, in whole or in part, through stream 12 to stream 15, and ultimately to second stage reactor 20.
  • Diesel product may be alternately recycled, in whole or in part, through stream 13 to stream 15, and ultimately to second stage reactor 20.
  • Bottoms material in stream 14 may be passed to further processing (in stream 14a) or, alternately, may be recycled in stream 14(b) to second reactor 20.
  • Second reactor 20 represents hydroprocessing zones subsequent to the first hydroprocessing zone. Each of these zones possesses an environment substantially free of H 2 S, NH 3 or other heteroatom components.
  • 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, heavy atmospheric gas oil, delayed coker gas oil, visbreaker gas oil demetallized oils, vacuum residua, atmospheric residua, deasphalted oil, Fischer-Tropsch streams, and FCC streams.
  • middle distillate fractions boiling in the range of about 250-700°F (121 -371 °C).
  • a middle distillate fraction is defined as having an approximate boiling range from about 250°F 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°F and 525°F (38-274°C).
  • the term "diesel boiling range” refers to hydrocarbons boiling in the range from 250°F to 700°F (121-371°C).
  • Gasoline and naphtha production is emphasized in the process of this invention.
  • Gasoline or naphtha normally boils in the range below 400°F (204°C), or C 10 -. 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.
  • Heavy hydrotreated gas oil another product of this invention, usually boils in the range from 550°F to 700°F.
  • Hydroprocessing conditions is a general term which refers primarily in this application to hydrocracking or hydrotreating, preferably hydrocracking.
  • the first stage reactor as depicted in Figure 1 , is a partial conversion hydrocracker.
  • Typical hydrocracking conditions include a reaction temperature of from 400°F-950°F (204°C-510°C), preferably 650°F-850°F (343°C-454°C).
  • Reaction pressure ranges from 500 to 5000 psig (3.5-4.5 MPa), preferably 1500-3500 psig (10.4-24.2 MPa).
  • LHSV ranges from 0.1 to 15 hf 1 (v/v), preferably 0.25-2.5 hr "1 .
  • Hydrogen consumption ranges from 500 to 2500 SCF per barrel of liquid hydrocarbon feed (89.1 -445m 3 H 2 /m 3 feed).
  • Reactors subsequent to the first hydroprocessing reactor are operated at a pressure at least 100 psig lower than that of the first reactor, and preferably from 500 to 1000 psig lower than the first reactor.
  • Each 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 VI, Group VII, or Group VIII metal or oxides or sulfides thereof, preferably one or more of iron, chromium, 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.
  • noble metals especially platinum and/or palladium, may be present as the hydrogenation component, either alone or in combination with the base metal hydrogenation components iron, chromium 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 usually is designed to remove sulfur and nitrogen and provide a degree of aromatic saturation. It will typically be a composite of a Group VI 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. Typically, such hydrotreating catalysts are presulfided.
  • Catalyst selection is dictated by process needs and product specifications.
  • a noble catalyst may be used in the second stage when there is a low amount of H 2 S present.
  • the Examples below demonstrate the relative effectiveness of recycling kerosene to produce lighter products of high quality, as opposed to not recycling kerosene.
  • the "recycle” of kerosene was simulated by passing kerosene from the first hydrocracking stage over the catalyst in the second hydrocracking stage.
  • the first stage kerosene possessed a smoke point of 14 mm and 25 LV% aromatics.

Landscapes

  • 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)

Abstract

L'invention concerne un processus à plusieurs étages permettant l'hydrocraquage des gasoils. Chaque étage comprend de préférence au moins une zone d'hydrocraquage. Le second étage et tous les étages suivants comprennent un milieu présentant une proportion réduite d'hétéroatomes. Des produits légers tels que le naphta, le kérosène et le diesel peuvent être recyclés après fractionnement (simultanément avec des produits légers provenant d'autres sources), vers le second étage (ou un des étages suivants) de manière à augmenter la production de produits plus légers tels que gaz et naphta. Les zones suivantes sont maintenues à une pression inférieure à celle de la première zone, de manière à réduire les charges d'exploitation.
PCT/US2003/013816 2002-06-04 2003-05-02 Hydrocraqueur a etages multiples avec recyclage de kerosene WO2003104358A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP03726599A EP1511824A4 (fr) 2002-06-04 2003-05-02 Hydrocraqueur a etages multiples avec recyclage de kerosene
JP2004511419A JP2006510746A (ja) 2002-06-04 2003-05-02 灯油再循環による多段式水素化分解
CA002487381A CA2487381A1 (fr) 2002-06-04 2003-05-02 Hydrocraqueur a etages multiples avec recyclage de kerosene
AU2003228827A AU2003228827B2 (en) 2002-06-04 2003-05-02 Multi-stage hydrocracker with kerosene recycle

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US10/162,774 US20030221990A1 (en) 2002-06-04 2002-06-04 Multi-stage hydrocracker with kerosene recycle
US10/162,774 2002-06-04

Publications (1)

Publication Number Publication Date
WO2003104358A1 true WO2003104358A1 (fr) 2003-12-18

Family

ID=29583629

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2003/013816 WO2003104358A1 (fr) 2002-06-04 2003-05-02 Hydrocraqueur a etages multiples avec recyclage de kerosene

Country Status (8)

Country Link
US (3) US20030221990A1 (fr)
EP (1) EP1511824A4 (fr)
JP (1) JP2006510746A (fr)
AU (1) AU2003228827B2 (fr)
CA (1) CA2487381A1 (fr)
PL (1) PL203817B1 (fr)
WO (1) WO2003104358A1 (fr)
ZA (1) ZA200409344B (fr)

Cited By (2)

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JP2008524390A (ja) * 2004-12-16 2008-07-10 シェブロン ユー．エス．エー． インコーポレイテッド 単一プロセスにおける燃料水素化分解及び留分供給原料の水素化脱硫
CN103572505A (zh) * 2012-08-08 2014-02-12 苏州维艾普新材料有限公司 一种纤维均匀分布用摇摆筒装置

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WO2006015169A2 (fr) * 2004-07-30 2006-02-09 Dictaphone Corporation Systeme et procede pour la fiabilite de niveau de rapports
CN101173189B (zh) * 2006-11-01 2010-05-12 中国石油化工股份有限公司 一种生产化工原料的两段加氢裂化方法
US7983170B2 (en) * 2006-12-19 2011-07-19 Citrix Systems, Inc. In-band quality-of-service signaling to endpoints that enforce traffic policies at traffic sources using policy messages piggybacked onto DiffServ bits
KR101399207B1 (ko) * 2007-08-22 2014-05-26 에스케이루브리컨츠 주식회사 미전환유를 이용한 고급 윤활기유 공급원료의 제조방법
US8658020B2 (en) 2007-12-19 2014-02-25 Phillips 66 Company Process for upgrading kerosene to gasoline by ring contraction—ring opening—dehydrogenation
US20090159493A1 (en) * 2007-12-21 2009-06-25 Chevron U.S.A. Inc. Targeted hydrogenation hydrocracking
US20100200459A1 (en) * 2009-02-10 2010-08-12 Chevron U.S.A. Inc. Selective staging hydrocracking
CN104043473B (zh) * 2013-03-13 2016-10-05 中国石油化工股份有限公司 一种加氢裂化催化剂及其应用
CN104043474B (zh) * 2013-03-13 2016-08-03 中国石油化工股份有限公司 一种加氢裂化催化剂及其制备方法和应用
WO2014149247A1 (fr) 2013-03-15 2014-09-25 Lummus Technology Inc. Hydrotraitement de produits craqués de façon thermique
US10010808B2 (en) * 2013-03-15 2018-07-03 Uop Llc Process and apparatus for recovering and blending hydroprocessed hydrocarbons and composition
CN105473690B (zh) 2013-07-02 2018-01-09 沙特基础工业公司 用于将原油转化成具有改进的碳效率的石化品的方法和设施
ES2725609T3 (es) * 2013-07-02 2019-09-25 Saudi Basic Ind Corp Proceso e instalación para la conversión de crudo en productos petroquímicos que tienen un rendimiento de etileno mejorado
WO2015128038A1 (fr) 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Procédé de conversion d'une charge d'hydrocarbures à point d'ébullition élevé en produits hydrocarbonés à point d'ébullition plus bas
SG11201606020PA (en) 2014-02-25 2016-08-30 Saudi Basic Ind Corp Process for converting hydrocarbons into olefins
CN104923291B (zh) * 2014-03-21 2018-07-31 中国石油化工股份有限公司 一种加氢裂化催化剂及其制备和应用
JP2018504387A (ja) 2014-12-22 2018-02-15 サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ Ｃ２およびｃ３炭化水素を製造するためのプロセス
CN107109257A (zh) * 2014-12-22 2017-08-29 沙特基础工业全球技术有限公司 用于生产c2和c3烃的方法
CN104611056B (zh) * 2015-02-11 2017-03-08 武汉凯迪工程技术研究总院有限公司 一种低温费托合成产物的加氢处理方法
US11041129B2 (en) * 2016-12-20 2021-06-22 Uop Llc Processes for producing a fuel range hydrocarbon and a lubricant base oil
US10550339B2 (en) * 2017-08-24 2020-02-04 Uop Llc Diesel and cycle oil upgrading process
US20200102510A1 (en) * 2018-09-29 2020-04-02 Uop Llc Process for maximizing production of heavy naphtha from a hydrocarbon stream
CN111088072A (zh) * 2018-10-24 2020-05-01 中国石油化工股份有限公司 一种降低重石脑油溴指数与增加航煤烟点的加氢裂化方法
US11572515B2 (en) * 2020-12-31 2023-02-07 Uop Llc Process for hydrocracking a hydrocarbon feed stream
US11859142B2 (en) * 2021-04-30 2024-01-02 Uop Llc Hydrocracking process for maximization of naphtha

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Publication number Priority date Publication date Assignee Title
JP2008524390A (ja) * 2004-12-16 2008-07-10 シェブロン ユー．エス．エー． インコーポレイテッド 単一プロセスにおける燃料水素化分解及び留分供給原料の水素化脱硫
CN103572505A (zh) * 2012-08-08 2014-02-12 苏州维艾普新材料有限公司 一种纤维均匀分布用摇摆筒装置

Also Published As

Publication number Publication date
US20030221990A1 (en) 2003-12-04
US20050103682A1 (en) 2005-05-19
AU2003228827B2 (en) 2008-11-20
PL203817B1 (pl) 2009-11-30
CA2487381A1 (fr) 2003-12-18
PL372757A1 (en) 2005-08-08
ZA200409344B (en) 2006-02-22
US20080283444A1 (en) 2008-11-20
JP2006510746A (ja) 2006-03-30
EP1511824A1 (fr) 2005-03-09
AU2003228827A1 (en) 2003-12-22
EP1511824A4 (fr) 2008-07-09

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