WO2012052042A1 - Procédé d'hydrocraquage d'une charge hydrocarbonée - Google Patents

Procédé d'hydrocraquage d'une charge hydrocarbonée Download PDF

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Publication number
WO2012052042A1
WO2012052042A1 PCT/EP2010/006411 EP2010006411W WO2012052042A1 WO 2012052042 A1 WO2012052042 A1 WO 2012052042A1 EP 2010006411 W EP2010006411 W EP 2010006411W WO 2012052042 A1 WO2012052042 A1 WO 2012052042A1
Authority
WO
WIPO (PCT)
Prior art keywords
bottom fraction
stripping
heavy bottom
heavy
hydrocracking
Prior art date
Application number
PCT/EP2010/006411
Other languages
English (en)
Inventor
Gordon Gongngai Low
Michael Glenn Hunter
Original Assignee
Haldor Topsøe A/S
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 Haldor Topsøe A/S filed Critical Haldor Topsøe A/S
Priority to PCT/EP2010/006411 priority Critical patent/WO2012052042A1/fr
Priority to BR112013008603A priority patent/BR112013008603A2/pt
Priority to PCT/EP2011/004949 priority patent/WO2012052116A2/fr
Priority to PL15166420.8T priority patent/PL2930225T3/pl
Priority to CA2813847A priority patent/CA2813847C/fr
Priority to EP15166420.8A priority patent/EP2930225B1/fr
Priority to US13/880,356 priority patent/US9580663B2/en
Priority to RU2013122685/04A priority patent/RU2588121C2/ru
Priority to KR1020137012369A priority patent/KR101608520B1/ko
Priority to MX2013004319A priority patent/MX2013004319A/es
Priority to HUE11773391A priority patent/HUE026597T2/hu
Priority to PT117733915T priority patent/PT2630218E/pt
Priority to CN201180050619.8A priority patent/CN103261374B/zh
Priority to ES15166420T priority patent/ES2959681T3/es
Priority to ES11773391.5T priority patent/ES2551608T3/es
Priority to PL11773391T priority patent/PL2630218T3/pl
Priority to EP11773391.5A priority patent/EP2630218B1/fr
Priority to ARP110103846A priority patent/AR084724A1/es
Publication of WO2012052042A1 publication Critical patent/WO2012052042A1/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
    • C10G65/12—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
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
    • C10G49/12—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles suspended in the oil, e.g. slurries
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/22—Separation of effluents

Definitions

  • the invention relates to a process for hydrocracking a hydrocarbon feedstock to obtain a more valuable lower boiling products such as liquefied petroleum gas ( LPG ) , naphtha, kerosene, and diesel.
  • LPG liquefied petroleum gas
  • the invention concerns a process whereby heavy polynuclear aromatic compounds are concentrated in a portion of the unconverted oil so they can be removed resulting in increased conversion and yield of products.
  • HPNA .heavy polynuclear aromatic
  • HPNA with 7+ aromatic rings are byproducts of hydrocracking reactions that can potentially cause significant problems in hydrocracking units.
  • solubility limit for the HPNA When the solubility limit for the HPNA is exceeded, solids form in transfer lines, valves and on heat exchanger surfaces.
  • HPNA can contribute to catalyst deactivation by reversible inhibition and coke formation.
  • HPNA problems particularly occur when processing heavy feedstocks with high distillation end- points and more aromatic cracked stocks in high conversion recycle units. Consequently, HPNA build up to high levels in the recycle streams normally employed in high conversion processes, resulting in fouling of the catalysts and equipment.
  • the conventional solution to this problem is to remove a portion of the recycle oil stream as an unconverted oil stream to purge the HPNA compounds from the system, effectively balancing the HPNA purge rate . Ah the rate of their formation by reactions. This approach limits the total conversion level achievable in the hydrocracker .
  • a hydrocarbonaceous heavy gas oil feedstock is combined with a hydrogen-rich gas and reacted over catalyst to obtain a hydrocracked effluent comprising of less dense, lower molecular weight products.
  • the hydrocracked effluent from the reactor is condensed and separated in a separation zone into a liquid portion comprising hydrocarbons and a vapour portion comprising un-reacted hydrogen.
  • the vapour from this separation may be combined with hydrogen makeup to account for hydrogen consumed by reaction and may then be compressed and re-circulated back to the reactor vessel.
  • the first liquid portion from the separation zone is then directed to a fractionation section where the lighter prod- ucts are distilled from the heavy unconverted products in a fractionation section e.g. a fractionation tower or a series of fractionation towers. Heat is normally input to this recovery operation in order to provide the necessary energy for separation.
  • the conventional approach to controlling the buildup of HPNA compounds in the recycle oil is to withdraw a purge of recycle oil product from the unit as unconverted oil.
  • the purge rate may be adjusted so as to balance the rejection of HPNA with the net production.
  • Such a purge essentially reduces the achievable total conversion level by hydro- cracking to less than 100 percent.
  • the purge rate can be from one or two percent up to as high as 10 percent of the fresh feed rate. The yield of valuable distillate products are correspondingly reduced at substantial economic loss to the refiner.
  • U.S. patent no. 6,361,683 discloses a hydrocracking process whereby the hydrocracked effluent is hydrogen stripped in a stripping zone to produce a gaseous hydrocarbonaceous stream which is passed through a post-treatment hydrogena- tion zone to saturate aromatic compounds.
  • the fractionation zone is associated with a stripping zone which is fed with stripped hydrocarbonaceous liquid obtained by stripping the hydrocracked effluent. Stripping to remove HPNA is also considered.
  • U.S. patent no. 6,858,128 discloses a hydrocracking process which utilises a fractionation zone that is divided to include sections suitable for steam stripping to concentrate HPNA.
  • U.S. patent no. 5,120,427 discloses a hydrocracking process in which a stripping column is provided as a stub column at the bottom of the fractionation zone, for recovering a ma- jority of light hydrocarbons, while enabling a purge of a liquid hydrocarbonaceous stream rich in HPNA.
  • a stripping column is provided as a stub column at the bottom of the fractionation zone, for recovering a ma- jority of light hydrocarbons, while enabling a purge of a liquid hydrocarbonaceous stream rich in HPNA.
  • HPNA poly-nuclear aromatic
  • the stream of heavy bottom fraction for stripping is heated prior to the stripping process to raise its temperature above its bubble point concentrat- ing the HPNA even further, by facilitating the evaporation of other constituents.
  • the first vapour portion comprises lighter low molecular weight products and unconverted hydrogen.
  • Another embodiment provides as the heavy bottom fraction the highest normal boiling fraction from the fractionation section, comprising hydrocarbonaceous material
  • improved separation is obtained in the counter current stripping column as it comprises multiple equilibrium stages in the form of trays or packing material .
  • a part of the heavy bottom fraction is directed into a stream of heavy bottom fraction for re- cycling being combined with the hydrocarbonaceous feedstock for being input to the hydrocracking zone, to provide hy- drocracking of unconverted oil.
  • the flow rate of the stream of heavy bot- torn fraction for stripping is controlled by a flow control unit according to a desired flow rate of the net purge of unconverted oil, such that the net purge flow may be optimised.
  • the hydrocarbonaceous feedstock may be hydrotreated prior to hydrocracking.
  • the energy for heating of the heavy bottom fraction for stripping is provided from heat exchange with one or more streams from the hydrocracking process e.g. a reactor effluent, or from heat exchange with an external source of heating medium such as high pressure steam, hot flue gas from a fired heater, or by electrical heating.
  • the hydrocracking process e.g. a reactor effluent
  • an external source of heating medium such as high pressure steam, hot flue gas from a fired heater, or by electrical heating.
  • An embodiment involves a process wherein the stripped liq- uid of heavy unconverted oil comprises heavy polynuclear aromatic compounds in an amount larger than the amount comprised in the heavy bottom fraction withdrawn from the fractionation column, thus reducing the share of unconverted oil in the net purge stream.
  • FIG. 1 illustrates an embodiment of the process according to the invention in which flow control is employed on a heavy bottom fraction for stripping and a part of the heavy bottom fraction is recycled.
  • the disclosed process utilizes specific process steps to reduce the net purge of unconverted oil from a hydro- cracker. This reduction may be accomplished by taking the bottom fraction stream from the bottom of the product fractionation section such as a fractionation column, heating it substantially above its bubble point and then stripping with steam in a counter-current column with fractionating trays or packing material.
  • the stripping step at elevated temperature vapourizes a substantial amount of the bottom fraction stream compared to simply stripping the heavy bot- torn fraction at its bubble point without heating.
  • the overhead vapour of the heavy bottom fraction may be returned to the fractionation section e.g. at the bottom.
  • the stripped part of the heavy bottom fraction remains a liquid and is collected in the bottom of the stripping tower. This stream is having a substantially higher boiling point than the original unconverted oil and therefore HPNA is concentrated in the heavier bottoms liquid which may then be removed as net purge from the hydrocracker.
  • the higher concentration of HPNA in the stripped liquid allows the removal of the required HPNA at lower purge rate.
  • the reduced purge rate results in higher total conversion in the hydrocracker together with increased yields of valuable distillate products.
  • This disclosure provides a simple process for concentrating the HPNA compounds in a portion of the unconverted oil stream and thereby minimizing the required purge flow rate.
  • the required purge flow rate is reduced substantially leading to higher conversion and better yields of final products .
  • the disclosure utilizes specific process steps to reduce the required purge of unconverted oil from the hydrocracker substantially, such as at least 25 percent and preferably by 50 percent or more. This reduction is accomplished by withdrawing a bottom fraction comprising unconverted oil in a first purge stream from the fractionation section, heating it substantially above its bubble point and then stripping with steam in a counter-current column with fractionating trays or packing material.
  • the stripping step va- pourizes a substantial amount, such as at least 25 percent and preferably by 50 percent or more of the bottom fraction stream returning the vapour to the bottom of the fractiona- tion section.
  • the remainder of the bottom fraction stream remains as liquid and is collected in the bottom of the stripping tower.
  • This liquid is substantially higher boiling than the original unconverted oil and as a consequence of the very high normal boiling point of the HPNA compounds, the physical separation concentrates the HPNA in the heavier bottoms liquid which is then removed as net purge from the hydrocracker .
  • the higher concentration of HPNA in the stripped liquid allows the removal of the required HPNA at lower purge flow rate.
  • the reduced purge rate results in higher total conversion in the hydrocracker together with increased yields of valuable distillate products .
  • Fresh feedstock consisting of a hydrocarbonaceous feed, such as petroleum or synthetic heavy gas oils of mineral or biological origin 1 is combined with hydrogen rich gas 2 and an optional recycle stream of unconverted product 16 and fed to a hydrocracking zone 3 consisting of one or more catalysts contained in one or more reaction vessels.
  • the catalysts promote the hydroconversion of the hydrocarbona- ceous feedstock, which may include hydrogenation to a lighter hydrocracked effluent.
  • the hydrocracking effluent comprising hydrocarbon products together with excess hydrogen not consumed by the reaction exits the hydrocracking zone 4 and enters a separation zone 5 consisting of one or more vessels that perform separation into a first vapour portion and a first liquid portion.
  • the first vapour portion 6 from the separation zone may be combined with makeup hydrogen 7 to replenish the hydrogen consumed by reaction.
  • the hydrogen rich stream may then be compressed in compressor 8 for recycle back to the hydrocracking zone.
  • the first liquid portion 9 from the separation step passes to a process heater 10 supplying energy for substantially vapourizing the fluid 11 before feeding the product fractionation section 12.
  • the fractionation section consists of one or more towers or columns with multiple equilibrium stages in the form of trays or packing material which may be operated in counter-current. The towers are normally stripped with steam or reboiled to facilitate vapourization of the products.
  • the fractionation section performs the separation of individual product and intermediate fractions 13, 14 such as gasoline, jet fuel and diesel fuel according to differences in their normal boiling points.
  • the heaviest bottom fraction i.e. unconverted oil 15 may be collected and withdrawn as an unconverted oil product or returned to the reactor in line 16 as a recycle oil stream for further conversion .
  • the aim of a hydrocracking process is to convert all or as much of the heaviest and highest molecular weight materials into products resulting in no or a minimal net yield of unconverted oil 15.
  • a first purge of unconverted oil or heavy bottom fraction 17 must be withdrawn from the hy- drocracker possibly on flow control 18 in order to avoid a build-up of HPNA within the reaction system.
  • the heavy bottom fraction stream for stripping is routed to a process heater 19 such that the temperature of the heated heavy bottom fraction stream for stripping 20 is raised substantially above the bubble point of the heavy bottom fraction stream for stripping and of the temperature of the fractionation section bottom.
  • This heated heavy bottom fraction stream for strip- ping is then fed to the top of a counter-current stripping tower 21 consisting of multiple equilibrium stages in the form of trays or packing material. Steam is added to the bottom of the stripping tower 22 to facilitate vapouriza- tion of the unconverted oil.
  • the overhead vapour from the top of the stripping tower 23 is routed to the bottom of the fractionating column 12.
  • the stripped heavy bottom fraction stream for stripping which is not vapourized in the stripper flows to the bottom of the tower and is then removed from the hydrocracker as a net purge (a necessary purge) of unconverted oil 24.
  • the operating conditions in the heavy bottom fraction stripping system are established such that the net purge of unconverted oil 24 from the bottom of the stripper is sub- stantially less than the heavy bottom fraction, i.e. unconverted oil 17 removed from the heavy bottom fraction stream for stripping, while sufficiently removing the undesired HPNA.
  • AST D-1160 apparatus Since this apparatus does not utilize reflux it generates a physical separation with substantial overlap between the overhead and bottoms product and correspond well to the vapour/liquid separation in a simple steam stripper.
  • Performance of the invention was evaluated based on a steam stripper under the conditions shown in Table 3 below.
  • Coronene HPNA molecule was also included in the experiment to show how the vapour-liquid equilibria would predict the distribution of the lightest HPNA species.
  • the results based on 350°C stripper feed temperature are presented in Table 4 below. At this feed temperature, 50 weight percent is distilled overhead and 50 percent is recovered in the bottoms liquid product. The coronene component has been concentrated in the stripper bottoms from 461 ppmwt in the feed to by 691 ppmwt in the bottoms corresponding to 150 percent .
  • the stripper results based on 380°C stripper feed temperature are presented in Table 5 below. At this feed temperature, 64 weight percent is distilled overhead and 36 percent is recovered in the bottoms liquid product. The coronene component has been concentrated in the stripper bottoms from 466 ppmwt in the feed to 727 ppmwt in the bottoms corresponding to 156 percent. Most of the HPNA molecules of concern in hydrocracker are in fact heavier and less volatile than coronene and can be expected to further concentrate in the stripper bottoms stream.

Abstract

Procédé d'hydrocraquage d'une charge hydrocarbonée comprenant les étapes suivantes : combinaison de la charge hydrocarbonée avec un gaz riche en hydrogène pour obtenir un mélange comprenant la charge hydrocarbonée et l'hydrogène ; (b) hydrocraquage catalytique du mélange comprenant la charge hydrocarbonée et l'hydrogène dans une zone d'hydrocraquage pour obtenir un effluent hydrocraqué ; (c) séparation de tout l'effluent hydrocraqué en une première fraction vapeur et une première fraction liquide dans la zone de séparation ; (d) chauffage de la première fraction liquide pour former une première fraction liquide vaporisée ; (e) introduction de la première fraction liquide vaporisée dans une section fractionnement pour obtenir des fractions de produits individuelles comprenant une fraction de fond lourde contenant l'huile non convertie au fond de la section fractionnement ; (f) soutirage à partir de la colonne de fractionnement de la fraction de fond lourde ; (g) transfert d'un flux de fraction de fond lourde à des fins de désessenciement; (h) désessenciement du flux de fraction de fond lourde à la vapeur, dans une colonne à désessencier à contre-courant pour former une vapeur de tête issue la fraction de fond lourde et une partie liquide désessenciée issue la fraction de fond lourde ; (i) chargement de la vapeur de tête issue de la fraction de fond lourde dans la section fractionnement ; et (j) soutirage de la partie liquide désessenciée issue de la fraction de fond lourde par le fond de la colonne à désessencier à contre-courant sous la forme d'une purge nette d'huile non convertie.
PCT/EP2010/006411 2010-10-20 2010-10-20 Procédé d'hydrocraquage d'une charge hydrocarbonée WO2012052042A1 (fr)

Priority Applications (18)

Application Number Priority Date Filing Date Title
PCT/EP2010/006411 WO2012052042A1 (fr) 2010-10-20 2010-10-20 Procédé d'hydrocraquage d'une charge hydrocarbonée
BR112013008603A BR112013008603A2 (pt) 2010-10-20 2011-10-05 processo para hidrocraquear uma matéria-prima de hidrocarboneto
PCT/EP2011/004949 WO2012052116A2 (fr) 2010-10-20 2011-10-05 Procédé d'hydrocraquage d'une charge hydrocarbonée
PL15166420.8T PL2930225T3 (pl) 2010-10-20 2011-10-05 Sposób hydrokrakowania surowca węglowodorowego
CA2813847A CA2813847C (fr) 2010-10-20 2011-10-05 Procede d'hydrocraquage d'une charge hydrocarbonee
EP15166420.8A EP2930225B1 (fr) 2010-10-20 2011-10-05 Procédé d'hydrocraquage d'une charge hydrocarbonée
US13/880,356 US9580663B2 (en) 2010-10-20 2011-10-05 Process for hydrocracking a hydrocarbon feedstock
RU2013122685/04A RU2588121C2 (ru) 2010-10-20 2011-10-05 Способ гидрокрекинга исходного углеводородного сырья
KR1020137012369A KR101608520B1 (ko) 2010-10-20 2011-10-05 탄화수소 공급원료의 수소화분해 방법
MX2013004319A MX2013004319A (es) 2010-10-20 2011-10-05 Proceso para hidrocraquear una materia prima de hidrocarburo.
HUE11773391A HUE026597T2 (hu) 2010-10-20 2011-10-05 Eljárás szénhidrogén nyersanyag hidrokrakkolására
PT117733915T PT2630218E (pt) 2010-10-20 2011-10-05 Processo para hidrocraquear uma matéria-prima de hidrocarboneto
CN201180050619.8A CN103261374B (zh) 2010-10-20 2011-10-05 用于氢化裂解烃进料的方法
ES15166420T ES2959681T3 (es) 2010-10-20 2011-10-05 Procedimiento para hidrocraquear una materia prima de alimentación hidrocarbonada
ES11773391.5T ES2551608T3 (es) 2010-10-20 2011-10-05 Procedimiento para hidrocraquear una materia prima de alimentación hidrocarbonada
PL11773391T PL2630218T3 (pl) 2010-10-20 2011-10-05 Sposób hydrokrakowania surowca węglowodorowego
EP11773391.5A EP2630218B1 (fr) 2010-10-20 2011-10-05 Procédé d'hydrocraquage d'une charge hydrocarbonée
ARP110103846A AR084724A1 (es) 2010-10-20 2011-10-18 Proceso para hidrocraquear una materia prima de hidrocarburo

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2010/006411 WO2012052042A1 (fr) 2010-10-20 2010-10-20 Procédé d'hydrocraquage d'une charge hydrocarbonée

Publications (1)

Publication Number Publication Date
WO2012052042A1 true WO2012052042A1 (fr) 2012-04-26

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PCT/EP2010/006411 WO2012052042A1 (fr) 2010-10-20 2010-10-20 Procédé d'hydrocraquage d'une charge hydrocarbonée

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016102302A1 (fr) 2014-12-22 2016-06-30 Axens Procede et dispositif pour la reduction des composes aromatiques polycycliques lourds dans les unites d'hydrocraquage
US9580663B2 (en) 2010-10-20 2017-02-28 Haldor Topsoe A/S Process for hydrocracking a hydrocarbon feedstock
CN107345162A (zh) * 2016-05-05 2017-11-14 中国石油化工股份有限公司 一种喷气燃料的生产方法
EP4105300A1 (fr) 2021-06-17 2022-12-21 Axens Procédé d hydrocraquage

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4961839A (en) * 1988-05-23 1990-10-09 Uop High conversion hydrocracking process
US5120427A (en) 1988-05-23 1992-06-09 Uop High conversion high vaporization hydrocracking process
US6361683B1 (en) 2000-02-22 2002-03-26 Uop Llc Hydrocracking process
US6858128B1 (en) 2000-04-25 2005-02-22 Uop Llc Hydrocracking process

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4961839A (en) * 1988-05-23 1990-10-09 Uop High conversion hydrocracking process
US5120427A (en) 1988-05-23 1992-06-09 Uop High conversion high vaporization hydrocracking process
US6361683B1 (en) 2000-02-22 2002-03-26 Uop Llc Hydrocracking process
US6858128B1 (en) 2000-04-25 2005-02-22 Uop Llc Hydrocracking process

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9580663B2 (en) 2010-10-20 2017-02-28 Haldor Topsoe A/S Process for hydrocracking a hydrocarbon feedstock
WO2016102302A1 (fr) 2014-12-22 2016-06-30 Axens Procede et dispositif pour la reduction des composes aromatiques polycycliques lourds dans les unites d'hydrocraquage
CN107345162A (zh) * 2016-05-05 2017-11-14 中国石油化工股份有限公司 一种喷气燃料的生产方法
CN107345162B (zh) * 2016-05-05 2019-02-22 中国石油化工股份有限公司 一种喷气燃料的生产方法
EP4105300A1 (fr) 2021-06-17 2022-12-21 Axens Procédé d hydrocraquage
FR3124189A1 (fr) 2021-06-17 2022-12-23 Axens Procédé d’hydrocraquage

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