WO2009003633A1 - Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène - Google Patents

Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène Download PDF

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Publication number
WO2009003633A1
WO2009003633A1 PCT/EP2008/005207 EP2008005207W WO2009003633A1 WO 2009003633 A1 WO2009003633 A1 WO 2009003633A1 EP 2008005207 W EP2008005207 W EP 2008005207W WO 2009003633 A1 WO2009003633 A1 WO 2009003633A1
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WO
WIPO (PCT)
Prior art keywords
distillation
zone
process according
sending
hydrocracking
Prior art date
Application number
PCT/EP2008/005207
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English (en)
Inventor
Alberto Delbianco
Nicoletta Panariti
Original Assignee
Eni S.P.A.
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 Eni S.P.A. filed Critical Eni S.P.A.
Priority to AP2010005118A priority Critical patent/AP3276A/xx
Priority to CA2691791A priority patent/CA2691791C/fr
Priority to BRPI0813301-8A2A priority patent/BRPI0813301A2/pt
Publication of WO2009003633A1 publication Critical patent/WO2009003633A1/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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • 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
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/063—Refinery processes
    • C01B2203/065—Refinery processes using hydrotreating, e.g. hydrogenation, hydrodesulfurisation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons

Definitions

  • the present invention relates to a high-productivity process for the total conversion to distillates alone, with no contextual production of fuel oil or coke, of heavy feedstocks, among which heavy crude oils also with a high metal content, distillation residues, heavy oils coming from catalytic treatment, "visbreaker tars", “thermal tars” , bitumens from "oil sands” possibly obtained from mining, liquids from different types of coal and other high-boiling feedstocks of a hydrocarbon nature, known as "black oils", also comprising hydrogenat- ing treatment in which hydrogen, self produced in the same process, is used.
  • the conversion of heavy feedstocks to liquid products can be substantially effected through two methods: one of the thermal type, the other based on hydrogenating treatment.
  • Thermal processes mainly coking and Visbreaking, have certain advantages as they allow feedstocks having a high polluting level to be fed.
  • the high production of coke and tar is such that its validity is greatly limited in some cases.
  • the poor quality of the distillates leads to the necessity of severe hydrogenating treatment to favour the removal of heteroatoms and bring the products to specification.
  • Visbreaking allows very low yields to distillates to be obtained together with low-quality products, ob- taining, on the contrary, high amounts of tar.
  • Coking in addition to having higher investment costs, also produces low-quality distillates and high quantities of coke.
  • the hydroconversion technologies currently used make use of fixed bed or ebullated bed reactors and adopt catalysts generally consisting of one or more transition metals (Mo, W, Ni, Co, etc.) supported on silica and/or alumina or another oxide support.
  • transition metals Mo, W, Ni, Co, etc.
  • ebullated bed processes were developed, wherein the catalytic bed, even if confined in a certain part of the reactor, is moveable and can expand due to the effect of the reagent flow in liquid and gaseous phase.
  • This allows the reactor to be equipped with mechanical apparatuses for removing the exhausted catalyst and feeding the fresh catalyst in continuous, without interrupting the running.
  • ebullated bed technologies can process heavy feedstocks with a metal content of up to 1,200 ppm Ni + V. Even if the ebullated bed technology benefits from the improvements provided by the continuous regeneration of the catalyst, it allows conversion levels to distillates of up to a maximum of 60% to be obtained.
  • Deasphaltation a liquid- liquid extraction treatment based on the use of paraffins, allows a variable aliquot of DAO, deasphalted oil, to be separated, which can have qualitative characteristics (in terms of metal content, carbonaceous residue, etc..) which are such as to favour the subsequent conversion.
  • This process has several advantages with respect to coking: significantly lower investment costs, the possibility of modulating the yield and quality of DAO and asphaltenes according to necessity, the production of a by-product (the same asphaltenes) which can be fed to the gasification process.
  • This residue can be di- rectly recycled to the initial fractionation column or to the deasphalting zone, from which, in addition to the as- phaltenes present in the feedstock, the side-products possibly formed in the hydrocracking phase can be removed, said by-products thus being used, at the same time self-producing the hydrogen necessary for the hydrogenat- ing treatment envisaged, by sending the asphaltene stream to a gasification section.
  • the new solution proposed herein allows the use of minimum concentrations of catalyst, which can be used only once, greatly simplifying the scheme; even at low catalyst concentrations, its formulation allows an optimal hydrogenation of the feedstock, preventing or minimizing the formation of coke .
  • the sending of the hydrotreatment residue to the deasphalting section allows the possible recovery of further quantities of DAO to be converted and, at the same time, to send the most concentrated fraction of pollut- ants (metals deriving from the feedstock, together with traces of catalyst) to gasification.
  • the process, object of the present invention for the conversion of heavy feedstocks, comprises the following steps : • sending the heavy feedstock to a first distillation zone (Dl) having one or more atmospheric and/or vacuum distillation steps whereby one or more light fractions are separated from the distillation residue; • sending the fraction consisting of the distillation residue of the first distillation zone (Dl) to a deasphalting zone (SDA) in the presence of solvents, obtaining two streams, one consisting of deasphalted oil (DAO) , the other containing asphaltenes; • sending the stream containing asphaltenes to a gasi- fication zone (POx) in order to obtain a mixture of H 2 and CO;
  • HCK hydrogen is introduced self-produced in the gasification area (POx) after separation in a gas separation (GS) zone from the mixture containing
  • the heavy feedstocks treated can be of different kinds: they can be selected from heavy feedstocks, dis- tillation residues, "heavy oils” from catalytic treatments, for example “unconverted oils” from hydrotreatment with fixed or ebullated beds, “heavy cycle oils” from catalytic cracking treatment, "thermal tars” (coming, for example, from visbreaking or similar thermal processes), bitumens from “oil sands” , different kinds of coals and any high-boiling feedstock of a hydrocarbon origin, generally known in the art as “black oils” .
  • the choice of sending the recycling of the distillation residue of the second distillation zone to the first distillation zone (Dl) and/or the deasphalting zone (SDA) is influenced by how the second distillation zone is effected: it is in fact preferable to send this residue completely, or at least partially, to the deasphalting area (SDA) if said second area consists of one or more atmospheric distillation steps.
  • the first distillation zone (Dl) preferably consists of one or more atmospheric distillation steps or one or more distillation steps and one vacuum step.
  • the heavier fraction of the light fractions separated in the first distillation zone can possibly be at least partially sent to the hydrocracking zone (HCK) .
  • HCK hydrocracking zone
  • the separation of H 2 from the mixture of H 2 and CO obtained from the gasification is preferably effected by means of molecular sieves.
  • a portion of the syngas stream, i.e. a mixture of H 2 and CO, obtained from the gasification, can be further upgraded as fuel for the generation of vapour or by combustion with combined cycles (IGCC) or it can be transformed into paraffin hydrocarbons through Fischer-Tropsch synthesis or it can be converted to methanol, dimethyl- ether, formaldehyde and, more generally, into the series of products deriving from Cl chemistry.
  • the distillation steps are preferably carried out at a reduced pressure ranging from 0.001 to 0.5 MPa, pref- erably between 0.1 and 0.3 MPa.
  • the deasphalting step (SDA) effected by means of extraction with a hydrocarbon or non-hydrocarbon solvent is generally carried out at temperatures ranging from 40 to 200 0 C and pressures of between 0.1 and 7 MPa. Furthermore, the same can be composed of one or more sections operating with the same solvent or different solvents; the recovery of the solvent can be carried out under sub-critical or super-critical conditions, with several steps, thus allowing a further fractionation be- tween deasphalted oil and resins.
  • the solvent of this deasphalting step is selected from light paraffins having from 3 to 6 carbon atoms, preferably from 4 to 5 carbon atoms, or a mixture of the same .
  • the hydrocracking (HCK) step is carried out in the presence of catalysts in slurry phase, preferably at temperatures ranging from 380 to 480 0 C, more preferably from 420 to 470 0 C, at a pressure ranging from 2 to 20 MPa, more preferably from 10 to 18 MPa.
  • Hydrogen is fed to the hydrocracking reactor which can operate both in the down- flow and, preferably, up- flow mode. This gas can be fed to different sections of the reactor.
  • the catalyst precursors used can be selected from those obtainable from easily decomposable oil-soluble precursors (metal naphthenates, metal derivatives of phosphonic acids, metal-carbonyls, etc..) or from preformed compounds based on one or more transition metals such as Ni, Co, Ru, W and Mo: the latter is preferred thanks to its higher catalytic activity.
  • the concentration of the catalyst defined according to the concentration of the metal or metals present in the hydrocracking reactor, ranges from 50 to 5,000 ppm, preferably from 50 to 900 ppm.
  • the process claimed therein allows the production of a completely deasphalted and demetallized "light syn- crude” (atmospheric and vacuum distillates) and also upgraded in terms of density, viscosity, CCR sulphur content.
  • An embodiment of the present invention is now pro- vided with the help of the enclosed figure 1, which should not be considered as limiting the scope of the invention itself.
  • the heavy feedstock (1) is fractionated in a first distillation zone (Dl) from which the light fractions are separated (2) and (3) from the distillation residue (4) .
  • the first distillation residue (4) is sent to a deasphalting unit (SDA) , said operation being effected by means of solvent extraction (8) .
  • SDA deasphalting unit
  • SDA deasphalting unit
  • DAO deasphalted oil
  • 10 the other containing asphaltenes
  • the stream containing asphaltenes (10) is sent to a gasification section (POx) in order to obtain syngas, i.e. a gaseous mixture of H 2 and CO (11) which is sent to a separation area (GS) , whereby a stream essentially consisting of CO (12) is separated and a stream essentially consisting of H 2 (13) which is sent to the hydrocracking step, another part (15) to the hydrotreatment step, thus providing the necessary quantity of hydrogen.
  • the stream (16) leaving the hydrocracking step (HCK) is sent to a second distillation zone (D2) .
  • the lighter fractions (D2i, D" 2 , D2 3/ ...D2 n ) are separated from the heavier fraction (19) at the bottom, which is recycled (20) to the first distillation zone (Dl) and/or (21) to the deasphalting zone (SDA) .
  • Example 1 Preparation of a deasphalted oil
  • the yield obtained using the procedure described above is equal to 89.8% by weight of deasphalted oil with respect to the starting residue.
  • Example 2 Hydrocracking of the deasphalted oil with n-pentane .
  • the system is pressurized with hydrogen and brought to temperature by means of an electrically heated oven; - during the reaction the system is kept under stirring by a swinging capillary system operating at a rotation rate of 900 rpm,- furthermore, the total pressure is kept constant by means of an automatic reintegration system of the hydrogen consumed; - at the end of the test, quenching of the reaction is effected; the autoclave is then depressurized and the gases collected in a sampling bag; the gaseous samples are then sent for gas chromatographic analysis; - the solids are separated from the products present in the reactor by filtration; the liquid products are analyzed in order to determine: the yields to distillates, sulphur content, nitrogen content, carbonaceous residue and metal content.
  • Example 3 Thermal cracking of the deasphalted oil with n-pentane .
  • the test was effected according to the operative procedure described in Example 2, without the addition of catalyst and by substituting hydrogen with nitrogen.
  • the reaction was carried out by feeding the feedstock produced in example 1, under the operative conditions indi- cated in Table 1.
  • the product distribution data are shown in Table 2.
  • Table 1 Operative conditions

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

L'invention concerne un processus de conversion de charges d'alimentation lourdes sélectionnées parmi les pétroles bruts lourd et extra lourd, des résidus de distillation de pétrole brut ou de traitement catalytique, des 'goudrons viscoréducteurs', des 'goudrons thermiques', des bitumes issus de 'sables pétrolifères', des liquide de charbons de différentes origines et d'autre charges d'alimentation à haut point d'ébullition d'origine hydrocarbure, appelées huiles noires, qui se caractérise en ce qu'il comprend les étapes suivantes : envoi de la charge d'alimentation lourde à une première zone de distillation (D1) possédant une ou plusieurs étapes de distillation sous vide et/ou à pression atmosphérique, une ou plusieurs fractions légères étant séparées du résidu de distillation, envoi de la fraction constituée du résidu de distillation de la première zone de distillation (D1) à une zone de désasphaltage (SDA) en présence de solvants, obtention de deux flux, l'un constitué de pétrole désasphalté ( DAO), l'autre contenant des asphaltènes, envoi du flux contenant des asphaltènes à une zone de gazéification (POx) afin d'obtenir un mélange de H2 et de CO, mélange du flux constitué de pétrole désasphalté (DAO) avec un catalyseur d'hydrogénation adapté et envoi du mélange obtenu à une zone d'hydrocraquage (HCK) dans laquelle de l'hydrogène est ajouté, auto-produit dans la zone de gazéification (POx) après avoir été séparé dans une zone de séparation de gaz (GS) du mélange contenant du CO, envoi du flux d'effluent de la zone d'hydrocraquage à une seconde zone de distillation (D2), constituée d'au moins une étape éclair et/ou une étape de distillation atmosphérique, à travers laquelle les différentes fractions sont séparées, venant de la réaction de l'hydrocraquage du résidu de distillation qui est recyclé à la première zone de distillation (D1) et/ou à la zone de désasphaltage (SDA).
PCT/EP2008/005207 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène WO2009003633A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AP2010005118A AP3276A (en) 2007-06-29 2008-06-17 Process for the conversion of heavy hydrocarbon feedstocks to distillates with the self-production of hydrogen
CA2691791A CA2691791C (fr) 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogene
BRPI0813301-8A2A BRPI0813301A2 (pt) 2007-06-29 2008-06-17 Processo para a conversão de cargas de alimentação pesadas a destilados.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT001303A ITMI20071303A1 (it) 2007-06-29 2007-06-29 Procedimento per la conversione di cariche idrocarburiche pesanti a distillati con autoproduzione di idrogeno
ITMI2007A001303 2007-06-29

Publications (1)

Publication Number Publication Date
WO2009003633A1 true WO2009003633A1 (fr) 2009-01-08

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ID=39766959

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PCT/EP2008/005207 WO2009003633A1 (fr) 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène

Country Status (5)

Country Link
AP (1) AP3276A (fr)
BR (1) BRPI0813301A2 (fr)
CA (1) CA2691791C (fr)
IT (1) ITMI20071303A1 (fr)
WO (1) WO2009003633A1 (fr)

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US8409541B2 (en) 2010-01-21 2013-04-02 Shell Oil Company Process for producing a copper thiometallate or a selenometallate material
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US8491784B2 (en) 2010-01-21 2013-07-23 Shell Oil Company Process for treating a hydrocarbon-containing feed
US8491782B2 (en) 2010-01-21 2013-07-23 Shell Oil Company Process for treating a hydrocarbon-containing feed
US8530370B2 (en) 2010-01-21 2013-09-10 Shell Oil Company Nano-tetrathiometallate or nano-tetraselenometallate material
US8562818B2 (en) 2010-01-21 2013-10-22 Shell Oil Company Hydrocarbon composition
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US8597608B2 (en) 2010-01-21 2013-12-03 Shell Oil Company Manganese tetrathiotungstate material
US8597499B2 (en) 2010-01-21 2013-12-03 Shell Oil Company Process for treating a hydrocarbon-containing feed
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US8940268B2 (en) 2010-01-21 2015-01-27 Shell Oil Company Process for producing a thiometallate or a selenometallate material
US8956585B2 (en) 2010-01-21 2015-02-17 Shell Oil Company Process for producing a thiometallate or a selenometallate material
US9011674B2 (en) 2010-12-10 2015-04-21 Shell Oil Company Process for treating a hydrocarbon-containing feed
US9440894B2 (en) 2013-03-14 2016-09-13 Lummus Technology Inc. Integration of residue hydrocracking and hydrotreating
WO2018232204A1 (fr) * 2017-06-15 2018-12-20 Saudi Arabian Oil Company Conversion d'hydrocarbures riches en carbone en hydrocarbures pauvres en carbone
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US10494578B2 (en) 2017-08-29 2019-12-03 Saudi Arabian Oil Company Integrated residuum hydrocracking and hydrofinishing
US11098264B2 (en) 2016-12-02 2021-08-24 Eni S.P.A. Process for producing lipids and other organic compounds from biomass
US11319498B2 (en) 2018-12-04 2022-05-03 Sabic Global Technologies B.V. Optimizing the simultaneous production of high-value chemicals and fuels from heavy hydrocarbons
RU2816582C2 (ru) * 2021-09-20 2024-04-02 Денис Анатольевич Устькачкинцев Способ определения избыточной доли легкой фракции нефти, образующейся при транспортировке и подготовке нефтегазоводяной смеси на установках подготовки и перекачки нефти

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US11041129B2 (en) * 2016-12-20 2021-06-22 Uop Llc Processes for producing a fuel range hydrocarbon and a lubricant base oil

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AP2010005118A0 (en) 2010-02-28
BRPI0813301A2 (pt) 2014-12-23
ITMI20071303A1 (it) 2008-12-30

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