EP0697455B1 - Procédé de préparation d'une cire hydrogénée - Google Patents

Procédé de préparation d'une cire hydrogénée Download PDF

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Publication number
EP0697455B1
EP0697455B1 EP19950202020 EP95202020A EP0697455B1 EP 0697455 B1 EP0697455 B1 EP 0697455B1 EP 19950202020 EP19950202020 EP 19950202020 EP 95202020 A EP95202020 A EP 95202020A EP 0697455 B1 EP0697455 B1 EP 0697455B1
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EP
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Prior art keywords
fraction
dao
hydrowax
residue
vacuum
Prior art date
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EP19950202020
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German (de)
English (en)
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EP0697455A3 (fr
EP0697455A2 (fr
Inventor
Jan Lodewijk Maria Dierickx
Johan Willem Gosselink
Nicolaas Mulder
Hennie Schaper
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Publication of EP0697455A2 publication Critical patent/EP0697455A2/fr
Publication of EP0697455A3 publication Critical patent/EP0697455A3/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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking

Definitions

  • the present invention relates to a process for producing a hydrowax which is very useful as a feedstock for a thermal steam cracker to produce lower olefins and as a feedstock for producing lubricating base oils.
  • Thermal steam cracking is a known method for producing lower olefins, particularly ethene and to a somewhat lesser extent propene. It is a strongly endothermic process and basically involves heating a hydrocarbon oil feed to a sufficiently high temperature for cracking reactions to occur followed by rapid cooling of the reactor effluent and fractionation of this effluent into the different products.
  • a steam cracker also commonly referred to as an ethene cracker, usually consists of a hot section and a cold section. The hot section consists of cracking furnaces, a cooling section and a primary fractionator for separating the effluent in a cracked residue, pan oil, cracked gas oil and cracked gas. Steam is introduced into the cracking furnace to dilute the feed.
  • the cracked gas is further separated into the various end products among which are pure ethene and propene.
  • this separation is achieved by first compressing the cracked gas from the primary fractionator to a pressure of about 30-40 bar followed by cooling the compressed gas to temperatures below -100 °C to enable separation into the various pure end products.
  • the removal of gases such as carbon dioxide and hydrogen sulphide also takes place in the cold section of the steam cracker. Because of the strong endothermic nature of the steam cracking process adequate and efficient heat recovery is very important in order to make the process economically viable.
  • a well known feedstock for the steam cracker is the naphtha fraction produced in the processing of crude oil. Atmospheric gas oils are also known as suitable cracker feedstocks.
  • a process for the production of lower olefins is disclosed involving the steam cracking of a hydrogenated gas oil feedstock, which is formed by the subsequent steps of thermal cracking of a hydrocarbon oil residue -suitably an atmospheric residue-, recovering a gas oil fraction by distillation from the thermal cracking effluent and catalytic hydrogenation of said gas oil fraction.
  • 1,922,665 a steam cracking process for preparing olefins is disclosed, wherein a dearomatised gas oil is used as the feedstock.
  • a dearomatised gas oil is used as the feedstock.
  • Important considerations in respect of the choice of the feedstock are, beside the potential ethene yield, chemical factors like the H/C ratio of the feed as well as economic factors such as the price of the feedstock and the stability of this price on the market.
  • Other factors such as availability of the feedstock, synergy potential of a steam cracker and a refinery and investments involved with integration of a steam cracker in a refinery also play an important role in choosing the appropriate feedstock.
  • hydrowax is an excellent steam cracker feedstock, inter alia because it has an attractive and relatively constant price, olefin yields are close to those for naphtha feedstocks and it offers excellent possibilities for integrating a steam cracker with a refinery.
  • fouling of the transfer line heat exchanger or TLE where high enthalpy heat is recovered from the hot effluent of the furnace for producing high pressure steam, is the major factor determining the run length of the steam cracker. This fouling is stated to be caused by the content of aromatic compounds in the hydrowax and by the tars formed during the pyrolysis in the cracking furnace.
  • the present invention aims to provide a process for the preparation of a hydrowax from hydrocarbon oil fractions heavier than flashed distillates, which hydrowax can be suitably applied as a feedstock in known steam cracking processes for producing lower olefins, particularly ethene, at a commercially attractive yield.
  • EP-A-0,280,476 another suitable process for producing lubricating base oils from a hydrowax is disclosed.
  • the hydrowax is hydroprocessed over a hydroprocessing catalyst comprising zeolite beta as an acidic component and a hydrogenation-dehydrogenation component, suitably platinum.
  • the hydroprocessed product is subsequently separated into a lower boiling fraction and a lubricating base oil raffinate, the latter being advantageously subjected to an aromatics extraction step, optionally followed by a hydrofinishing step, to yield the lubricating base oil.
  • the present invention also aims to provide a process wherein a hydrowax is prepared which can be very suitably used as a feedstock for producing lubricating base oils. Accordingly, the present invention aims to provide a process, wherein the hydrowax prepared is a suitable feedstock for a dewaxing unit or a hydroprocessing unit.
  • the present invention relates to a process for producing a hydrowax comprising the steps of
  • the blend of DAO and distillate fraction(s) should have a sufficiently low heavy metal content. Therefore the heavy metal content of the hydrocracker feedstock should be reduced prior to hydrocracking. This implies that either the DAO is hydrodemetallised before being blended with the distillate fraction(s) or the blend of DAO and distillate fraction(s) is hydrodemetallised prior to being subjected to hydrocracking. In practice the first option, i.e.
  • hydrodemetallisation of the DAO will be preferred, because all or almost all of the heavy metal present in the blend of DAO and distillate fraction(s) was originally contained in the DAO anyway, so that it is economically more effective to hydrodemetallise the DAO where the DAO has been derived from a crude oil in which heavy metals are naturally occurring in relatively high amounts, the DAO is likely to have a high heavy metal content as well. Additionally, if the deasphalting depth in the deasphalting treatment is high, i.e. only the most heavy asphaltenic components are removed, then the DAO will still contain substantial amounts of heavy metals as compared with the deasphalting feed. If, on the other hand, said depth is relatively low, i.e. beside the heavy asphaltenic components some lighter asphaltenes have been removed as well, then the heavy metals content in the DAO will be significantly lower than the heavy metals content of the deasphalting feed.
  • hydrowax which is a suitable feedstock for a steam cracker.
  • hydrowax should be produced from flashed distillate fractions only, since the use of heavier fractions would cause too much fouling in the TLE, thus imposing an economically unacceptable run time constraint on the steam cracker.
  • the hydrowax obtained as the top-fraction can very suitably be used as the feedstock for a steam cracker in order to produce ethene and propene or as a feedstock for a dewaxing or hydroprocessing unit for producing lubricating base oils.
  • the blending or weight ratio of distillate fraction(s) to DAO, which optionally has been hydrodemetallised, is not particularly critical and is primarily determined by hydrocracker constraints.
  • this weight ratio is suitably in the range of from 20/80 to 80/20 and preferably from 40/60 to 70/30.
  • Hydrocracking of the blend of distillate fraction(s) and optionally hydrodemetallised DAO may be performed in any suitable way known in the art. Generally, hydrocracking is carried out in the presence of hydrogen and a suitable hydrocracking catalyst at elevated temperature and pressure. Hydrocracking catalysts usually consist of one or more metals from nickel, tungsten, cobalt and molybdenum in elemental, oxidic or sulphidic form on a suitable carrier such as alumina, silica, silica-alumina or a zeolite. There are many commercially available hydrocracking catalysts, which can be suitably applied in the process according to the present invention.
  • the hydrocracking process can be a single- or a multiple-staged process, whereby a single-staged process is preferred because multiple-staged hydrocracking causes deeper hydrogenation of polyaromatics, thus producing more polynaphthenes.
  • Such polynaphthenes produce more fuels and tar and less olefins than a hydrowax resulting from a single-stage hydrocracking process.
  • a stacked bed of a hydrodenitrification/first-stage hydrocracking catalyst on top of a conversion catalyst can suitably be used.
  • Particularly suitable hydrodenitrification/first-stage hydrocracking catalysts are NiMo/alumina and CoMo/alumina, optionally promoted with phosphorus and/or fluorine.
  • Suitable conversion catalysts include those based on a Group VIB metal, a Group VIII metal and an acidic carrier.
  • a promoter in the form of phosphorus (P) may be present as well.
  • Concrete examples of such catalysts are NiW/zeolite, NiW/silica-alumina and NiW/zeolite/silica-alumina.
  • Common hydrocracking conditions are an operating pressure of 80-250 bar, suitably 100-200 bar, and an operating temperature of 300-500 °C, suitably 350-475 °C.
  • the distillate fractions useful in the process of the present invention may be either heavy gas oil fractions obtained from the atmospheric distillation of a crude oil or flashed distillate fractions obtained from the vacuum flash distillation or vacuum distillation of an atmospheric hydrocarbon oil residue.
  • the DAO used is suitably obtained by deasphalting a residual hydrocarbon oil, preferably a vacuum residue.
  • the deasphalting may be carried out in any conventional manner.
  • a well known and suitable deasphalting method is solvent deasphalting, which involves the countercurrent treatment of the residual hydrocarbon oil feed with an extracting solvent.
  • This extracting solvent usually is a light hydrocarbon solvent containing paraffinic compounds having 3 to 8 carbon atoms, such as propane, butane, isobutane, pentane, isopentane, hexane and mixtures of two or more of these.
  • Preferred paraffinic hydrocarbons are those having 3 to 5 carbon atoms with butane, pentane and mixtures thereof being most preferred.
  • the solvent deasphalting treatment is conveniently carried out in a rotating disc contactor or a plate column with the residual hydrocarbon oil feed entering at the top and the extracting solvent entering at the bottom.
  • the lighter hydrocarbons present in the residual hydrocarbon oil dissolve in the extracting solvent and are withdrawn at the top of the apparatus. From this top-fraction, the DAO is obtained after recovery of the extracting solvent.
  • the asphaltenes, which are insoluble in the extracting solvent are withdrawn at the bottom of the apparatus.
  • deasphalting is carried out at a total extracting solvent to residual hydrocarbon oil ratio of 1.5 to 8 wt/wt, a pressure of 1 to 50 bar and a temperature of 160 to 230 °C.
  • Hydrodemetallisation of either the DAO or the blend thereof with distillate fraction(s) can be achieved by any hydrodemetallisation method known in the art.
  • such method involves passing the feed to be treated in an upward, downward or radial direction through one or more vertically disposed reactors containing a fixed or moving bed of hydrodemetallisation catalyst particles at an elevated temperature and pressure in the presence of hydrogen.
  • Well known demetallisation operations are the bunker flow operation, the fixed bed operation, the fixed bed swing operation and the movable bed operation.
  • Suitable catalysts usually consist of oxidic carriers such as alumina, silica or silica-alumina, on which one or more metals of Group VIB or VIII of the Periodic Table of Elements may be deposited either in elemental form or as a metal compound.
  • Such hydrodemetallisation catalysts are commercially available from many catalyst suppliers. Particularly suitable catalysts are those having as the active agent one of the combinations NiMo or CoMo, optionally promoted with phosphorus (P), on an alumina carrier. It is well known that the type of catalysts described hereinbefore in practice will also exhibit some upgrading activity in terms of hydrodenitrification and/or hydrodesulphurization, removal of heavy hydrocarbons and conversion of hydrocarbons having a boiling point above 520 °C into components having a lower boiling point.
  • Hydrodemetallisation is usually carried out at a hydrogen partial pressure of 20-250 bar, a temperature of 300-470 °C, preferably 310-440 °C, and a space velocity of 0.1-10 l/l.hr, preferably 0.2-7 l/l.hr.
  • the DAO used is produced by deasphalting a vacuum hydrocarbon oil residue, optionally followed by hydrodemetallisation.
  • a vacuum hydrocarbon oil residue is obtained as the residual fraction of the vacuum distillation of an atmospheric hydrocarbon oil residue.
  • the distillate fraction(s) used in the process according to the present invention are preferably obtained from the vacuum distillation of an atmospheric hydrocarbon oil residue as well.
  • said vacuum hydrocarbon oil residue from which the DAO is produced is derived from the same atmospheric hydrocarbon oil residue as said distillate fraction(s).
  • Separation of the 370+ fraction from the hydrocracker effluent can be achieved by means of fractionation devices commonly applied in hydrocracker units.
  • the separation in step (c) can also be performed by any method known in the art for separating a hydrocarbon oil feed into two or more different fractions based on the boiling points of the various components present in said hydrocarbon oil feed. Examples of suitable separation methods include distillation at atmospheric or reduced pressure, such as conducted in a mid vacuum flasher or a high vacuum distillation unit.
  • the only important parameter in this respect for the purpose of the present invention is the effective cutpoint, i.e. the temperature indicating the boiling point of the highest boiling components of the top-fraction and the lowest boiling components of the bottom-fraction.
  • this will mean that at least 85% by weight, preferably at least 90% by weight and most preferably at least 95% by weight, of the components constituting the top-fraction has a boiling point below the effective cutpoint, while at least 70% by weight of the components constituting the bottom-fraction has a boiling point above the effective cutpoint.
  • the effective cutpoint must be below 600 °C and preferably below 580 °C.
  • the effective cutpoint is above 400 °C and more preferably above 450 °C. From a yield perspective, it will usually be even more preferred to use an effective cutpoint above 500 °C and most preferably above 550 °C, because -as will be generally appreciated- a lower effective cutpoint goes at the expense of the hydrowax yield.
  • a lower effective cutpoint should be chosen.
  • the hydrowax is eventually obtained in step (c) as the top-fraction and can be used directly as feed for a steam cracker or as feed for a process line-up for producing lubricating base oils.
  • the bottom-fraction contains many heavy hydrocarbonaceous compounds, partly polyaromatic ring-structures.
  • at least a part of the bottom-fraction obtained in step (c) may be blended with the optionally hydrodemetallised DAO prior to hydrocracking. In this way an optimum hydrowax yield can be realised.
  • Additional efficiency increasing measures include for instance recycling at least a part of the cracked residue and/or the cracked gas oil fraction obtained from the steam cracker to the inlet of the deasphalter and/or to the inlet of the hydrodemetallisation reactor, if the DAO is hydrodemetallised.
  • the present invention also relates to use of the hydrowax obtainable by the process according to the present invention both as the feed in thermal steam cracking for producing lower olefins and as the feed in the production of lubricating base oils.
  • Figure 1 illustrates how a preferred embodiment of the process according to the present invention can be integrated in a refinery-steam cracker line-up or in a refinery having lubricating base oil production facilities.
  • a crude oil (9) is passed into atmospheric distillation unit (1), where it is separated into atmospheric residue (11) and distillate fractions (10).
  • the atmospheric residue (11) is subjected to vacuum flash distillation in vacuum flash distillation unit (2) and separated into one or more (vacuum) flashed distillate fractions (16) and vacuum residue (12).
  • Vacuum residue (12) is subsequently passed into deasphalting zone (3) resulting in asphaltic fraction (14) and DAO (13), which is hydrodemetallised in hydrodemetallisation unit (4).
  • the hydrodemetallised DAO (15) is blended with distillate fraction(s) (16) and the resulting blend stream is subjected to hydrocracking in hydrocracker (5).
  • the hydrocracker effluent (17) is separated in fractionator (6) into top-fraction (18) and 370+ bottom-fraction (19). This 370+ fraction is separated in (high) vacuum distillation unit (7) into hydrowax (20) and bottom-fraction (23), part of which may be blended with hydrodemetallised DAO (15). This is indicated with a dotted line.
  • the hydrowax (20) is used as the feed for steam cracker (8), thus producing ethene (21).
  • the hydrowax (20) is used as the feed for lubricating base oil production facility (8), thus producing lubricating base oil(s) (21).
  • the invention is further illustrated by the following example.
  • a flashed distillate FD having the properties as listed in Table I was blended with a hydrodemetallised DAO (DAO+) in a weight ratio of FD:DAO+ of 55:45.
  • the DAO+ was obtained by passing a DAO (obtained by subjecting vacuum residue to butane deasphalting at 70 %wt yield; properties listed in Table I) over a conventional hydrodemetallisation catalyst (NiMoP on alumina) under the conditions specified in Table II.
  • the resulting FD/DAO+ blend was subjected to hydrocracking over a stacked bed of a conventional first stage hydrocracking catalyst (NiMoP on alumina) on top of a dedicated second stage hydrocracking catalyst (NiW on amorphous silica-alumina) under the conditions listed in Table II.
  • the hydrocracker effluent was separated in a fractionator into a top-fraction and a 370+ bottom-fraction. This 370+ fraction was then separated in a vacuum flasher at an effective cutpoint of 576 °C into a hydrowax (the top fraction) and a bottom fraction.
  • the properties of the hydrowax are also given Table I.
  • the hydrowax was subsequently passed into a steamcracking unit.
  • the steamcracking unit was operated at a temperature of 820 °C, an outlet pressure of 2.15 bar, a feed flow of 49.6 g/h and a gas flow of 43.8 Nl/h.
  • Ethene yield was 28.0 %wt and propene yield was 13.8 %wt, both weight percentages being based on weight of feed.

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

Claims (10)

  1. Procédé de production d'une hydrocire comprenant les étapes :
    (a) d'hydrocraquage d'un mélange obtenu en mélangeant au moins une fraction de distillat, obtenue d'une unité de fractionnement (2), et une huile désasphaltée (DAO) dans lequel soit le mélange, soit la DAO a été hydrodémétallisé avant l'hydrocraquage;
    (b) de séparation de l'effluent de l'hydrocraqueur d'une fraction dont au moins 90% en poids ont un point d'ébullition de 370°C ou plus (la fraction 370+); et
    (c) de séparation, dans un séparateur (7), de la fraction 370+ en une fraction de tête et une fraction de queue à un point de coupe effectif en dessous de 600°C, en donnant ainsi l'hydrocire comme fraction de tête.
  2. Procédé suivant la revendication 1, dans lequel la DAO est hydrodémétallisée avant d'être mélangée avec la ou les fractions de distillat.
  3. Procédé suivant l'une ou l'autre des revendications 1 et 2, dans lequel le rapport en poids fraction(s) de distillat à la DAO éventuellement hydrodémétallisée dans le mélange à hydrocraquer se situe dans la gamme de 20/80 à 80/20, et avantageusement de 40/60 à 70/30.
  4. Procédé suivant l'une quelconque des revendications précédentes, dans lequel la ou les fractions de distillat sont produites par une distillation par détente sous vide d'un résidu d'huile hydrocarbonée atmosphérique.
  5. Procédé suivant l'une quelconque des revendications précédentes, dans lequel la DAO est produite par désasphaltage d'un résidu d'huile hydrocarbonée sous vide.
  6. Procédé suivant l'une ou l'autre des revendications 4 et 5, dans lequel le résidu d'huile hydrocarbonée sous vide de la revendication 5 est produit à partir du même résidu d'huile hydrocarbonée atmosphérique que la ou les fractions de distillat de la revendication 4.
  7. Procédé suivant l'une quelconque des revendications précédentes, dans lequel le point de coupe effectif dans l'étape (c) se situe dans l'intervalle de 400 à 560°C, avantageusement de 450 à 520°C.
  8. Procédé suivant l'une quelconque des revendications précédentes, dans lequel au moins une partie de la fraction de queue obtenue dans l'étape (c) est mélangée à la DAO éventuellement hydrodémétallisée avant l'hydrocraquage.
  9. Utilisation de l'hydrocire obtenable par le procédé suivant l'une quelconque des revendications 1 à 8, comme alimentation dans un vapocraquage thermique pour la production d'oléfines inférieures, ou comme alimentation pour la production d'huiles de base lubrifiantes.
  10. Raffinerie avec hydrocraqueur intégrée avec un vapocraqueur ou avec un système de traitement pour la production d'huiles de base lubrifiantes, dans laquelle l'alimentation pour le vapocraqueur ou le système de traitement précité est produite dans la raffinerie avec hydrocraqueur utilisée suivant le procédé de l'une quelconque des revendications 1 à 8, laquelle raffinerie comprend une unité de distillation atmosphérique (1) pouvant recevoir une huile brute (9) et la séparer en un résidu atmosphérique (11) et des fractions de distillat (10), une unité de distillation par détente sous vide (2) adaptée pour recevoir le résidu atmosphérique (11) et le séparer en une ou plusieurs fractions de distillat de détente (16) et un résidu sous vide (12), une zone de désasphaltage (3) pouvant désasphalter le résidu sous vide (12) et produire une fraction asphaltique (14) et une DAO (13), une unité d'hydrodémétallisation (4) pouvant démétalliser la DAO (13), un hydrocraqueur (5) adapté pour recevoir un mélange de DAO hydrodémétallisée (15) et une ou des fractions de distillat (16), une unité de fractionnement (6) pouvant séparer l'effluent d'hydrocraqueur (17) en une fraction de tête (18) et une fraction de queue 370+ (19), une unité de distillation sous vide (7) pouvant séparer la fraction 370+ en une hydrocire (20) et une fraction de queue (23), et un vapocraqueur ou un dispositif de production d'huiles de base lubrifiantes, installation (8) pouvant recevoir l'hydrocire (20) comme alimentation et produire en particulier des oléfines inférieures ou de l'huile de base lubrifiante (12).
EP19950202020 1994-07-22 1995-07-21 Procédé de préparation d'une cire hydrogénée Expired - Lifetime EP0697455B1 (fr)

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Application Number Priority Date Filing Date Title
EP19950202020 EP0697455B1 (fr) 1994-07-22 1995-07-21 Procédé de préparation d'une cire hydrogénée

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Application Number Priority Date Filing Date Title
EP94202148 1994-07-22
EP94202148 1994-07-22
EP19950202020 EP0697455B1 (fr) 1994-07-22 1995-07-21 Procédé de préparation d'une cire hydrogénée

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EP0697455A2 EP0697455A2 (fr) 1996-02-21
EP0697455A3 EP0697455A3 (fr) 1996-05-01
EP0697455B1 true EP0697455B1 (fr) 2001-09-19

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Cited By (1)

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Publication number Priority date Publication date Assignee Title
US11814590B2 (en) 2021-08-27 2023-11-14 Sk Innovation Co., Ltd. Method of producing lubricating base oil from atmospheric residue in pyrolysis oil derived from waste plastic

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FR2864103B1 (fr) * 2003-12-23 2006-03-17 Inst Francais Du Petrole Procede de traitement d'une charge hydrocarbonee incluant un enlevement des resines
WO2014095813A1 (fr) 2012-12-17 2014-06-26 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'une hydrocire
CN105849237A (zh) * 2013-12-24 2016-08-10 国际壳牌研究有限公司 生产中间馏分油的方法
EA037443B1 (ru) 2015-11-30 2021-03-29 Сабик Глобал Текнолоджис Б.В. Способ получения высококачественного исходного материала для процесса парового крекинга
AR110493A1 (es) 2016-12-08 2019-04-03 Shell Int Research Un método para pretratar y convertir hidrocarburos
CN110461999A (zh) * 2017-02-02 2019-11-15 沙特基础全球技术有限公司 一种制备用于加氢处理单元的原料的方法和一种直接加工原油以生产烯属和芳族石化产品的集成加氢处理和蒸汽热解的方法
KR20210154152A (ko) 2019-04-18 2021-12-20 쉘 인터내셔날 리써취 마트샤피지 비.브이. 지방족 탄화수소의 회수

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GB1537822A (en) 1975-01-22 1979-01-04 Shell Int Research Process for the production of normally gaseous olefins
CA1222471A (fr) * 1985-06-28 1987-06-02 H. John Woods Methode pour ameliorer le rendement des produits distillables dans le craquage a diluant donneur d'hydrogene
GB8629476D0 (en) * 1986-12-10 1987-01-21 Shell Int Research Manufacture of lubricating base oils
US4764266A (en) 1987-02-26 1988-08-16 Mobil Oil Corporation Integrated hydroprocessing scheme for production of premium quality distillates and lubricants
ES2021720B3 (es) * 1987-09-28 1991-11-16 Uop (A New York General Partnership) Control de productos aromaticos polinucleares en un proceso de hidrofraccionamiento

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11814590B2 (en) 2021-08-27 2023-11-14 Sk Innovation Co., Ltd. Method of producing lubricating base oil from atmospheric residue in pyrolysis oil derived from waste plastic

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EP0697455A2 (fr) 1996-02-21

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