WO2009003634A1 - 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
WO2009003634A1
WO2009003634A1 PCT/EP2008/005210 EP2008005210W WO2009003634A1 WO 2009003634 A1 WO2009003634 A1 WO 2009003634A1 EP 2008005210 W EP2008005210 W EP 2008005210W WO 2009003634 A1 WO2009003634 A1 WO 2009003634A1
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zone
distillation
process according
sending
hydrotreatment
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PCT/EP2008/005210
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English (en)
Inventor
Alberto Delbianco
Nicoletta Panariti
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Eni S.P.A.
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Priority to BRPI0813945-8A2A priority Critical patent/BRPI0813945A2/pt
Priority to CA2691794A priority patent/CA2691794C/fr
Priority to AP2010005119A priority patent/AP2845A/xx
Publication of WO2009003634A1 publication Critical patent/WO2009003634A1/fr

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    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • 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
    • 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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • 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
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/33—Laboratory scale gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0966—Hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]

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 prod- ucts 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 of 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.
  • This latter element represents a very critical factor, mainly in certain cases in which there is a limited availability of natural gas. It can therefore be impor- tant to produce hydrogen starting from alternative sources, for example through the gasification of byproducts such as coke, residues, tar, asphaltenes, etc..
  • 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 in- vestment 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.
  • deasphalting does not produce distil- lates : it is therefore necessary to subject the DAO to subsequent cracking treatment .
  • This residue can be directly 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 re- moved, 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 to gasification the most concentrated fraction of pollutants (metals deriving from the feedstock, together with traces of catalyst) .
  • the process, object of the present invention, for the conversion of heavy feedstocks comprises the following steps:
  • the heavy feedstocks treated can be of different kinds: they can be selected from heavy feedstocks, distillation residues, "heavy oils” from distillation resi- dues, 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.
  • a separation of said effluent stream is preferably effected by means of separators in order to obtain a gaseous phase and a liquid phase to be sent to the hy- drotreatment zone (HT) and to the second distillation zone (D2) , respectively.
  • 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 fraction sent to the hydrotreatment zone (HT) is preferably the lighter stream from the single step or from the last distillation step.
  • the gasification can be effected by feeding the stream containing asphaltenes to the gasifier, together with oxygen and vapour which react under exothermic con- ditions at a temperature of over 1,300 0 C and a pressure ranging from 30 to 80 bar, to produce mainly H 2 and CO.
  • 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 mixture of H 2 and CO obtained in the gasifica- tion zone (POx) is sent to a water-gas-shift zone (WGS) to generate hydrogen by reaction with water.
  • the same paraffin hydrocarbons obtained through Fischer-Tropsch can be mixed to the various cuts obtained from the distillation or flash step, improving the compo- sitional characteristics.
  • the hydrotreatment step (HT) is preferably carried out at a temperature ranging from 360 to 450 0 C, preferably from 380 to 440 0 C, at a pressure of between 3 and 30 MPa, preferably between 10 and 20 MPa.
  • Hydrogen is fed to the hydrotreatment reactor which can operate in the down-flow or, preferably, up-flow mode. This gas can be fed to several sections of the reactor.
  • the distillation steps are preferably carried out at a reduced pressure ranging from 0.001 to 0.5 MPa, preferably between 0.1 and 0.3 MPa.
  • the hydrotreatment step (HT) can consist of one or more fixed bed reactors operating within the range of conditions mentioned above. A portion of the distillates produced in the first reactor can be recycled to the sub- sequent reactors of the same step.
  • 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.
  • 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 between deasphalted oil and resins. It is advisable for the solvent of this deasphalting step to be 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.
  • 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 allows the production of a com- pletely deasphalted and demetallized "light syncrude” (atmospheric and vacuum distillates) and also upgraded in terms of density, viscosity, CCR sulphur content.
  • 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 lighter fraction (2) separated in the first distillation zone (Dl) is mixed with the catalyst (5) to form the stream (6) fed to the hydrotreating (HT) reactor.
  • the stream (7) leaving the hydrotreatment step (HT) is sent to a second distillation zone (D2) .
  • 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
  • Two streams are obtained from the deasphalting unit (SDA) : one (9) consisting of deasphalted oil (DAO) , the other containing asphaltenes (10) .
  • DAO deasphalted oil
  • 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 con- sisting of CO (12) is separated and a stream essentially consisting of H 2 (13) of which a part (14) is sent to the hydrocracking step, another part (15) to the hydrotreatment step, thus providing the necessary quantity of hydrogen for effecting the hydrocracking and hydrotreatment reactions.
  • the stream (16) leaving the hydrocracking step (HCK) is either sent (17) to the hydrotreatment step (HT) or it is sent (18) to the 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) .
  • At least part (22) of the heavier light fraction (3) , separated in the first distillation zone (Dl) can possibly be sent to the hydrocracking (HCK) zone.
  • the mixture of feedstock and solvent is heated to a tem- perature of 180 0 C, with stirring (800 rpm) by means of a mechanical stirrer for a period of 30 minutes.
  • the two phases are decanted and separated, the asphaltene phase which is deposited on the bottom of the autoclave and the deasphalted oil phase di- luted in the solvent.
  • the decanting lasts for about two hours.
  • the DAO-solvent phase is then transferred to a second tank, by means of a suitable recovery system.
  • the DAO-pentane phase is subsequently recovered, and the solvent is then eliminated by evaporation.
  • 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 test was effected making use of a stirred micro- autoclave of 30 cm 3 , according to the following general operative procedure:
  • 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;
  • 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.

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  • Chemical & Material Sciences (AREA)
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  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (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 seule fraction légère ou d'une ou de plusieurs fractions légères venant de la première zone de distillation (D1) à une zone d'hydrotraitement (HT) où de l'hydrogène est introduit, 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 d'effluent de la zone d'hydrotraitement à une seconde zone de distillation (D2), constituée d'au moins une étape éclair et/ou d'une étape de distillation atmosphérique, à travers laquelle les différentes fractions sont séparées, venant de l'hydrotraitement du résidu de distillation qui est recyclé à la première zone de distillation (D1) et/ou à la zone de désasphaltage (SDA), mélange du flux constitué du pétrole désasphalté (DAO) avec un catalyseur d'hydrogénation et envoi du mélange obtenu à une zone d'hydrocraquage (HCK) dans laquelle de l'hydrogène est ajouté, et de laquelle le flux d'effluent est envoyé à la zone d'hydrotraitement (HT) et/ou à la seconde zone de distillation (D2), envoi du flux contenant des asphaltènes vers une zone de gazéification (POx) afin d'obtenir un mélange de H2 et de CO; envoi du mélange de H2 et de CO obtenu dans la zone de gazéification (POx) dans une zone de séparation de gaz (GS) pour récupérer l'hydrogène à utiliser comme atmosphère réactive pour les sections d'hydrotraitement (HT) et d'hydrocraquage (KCK).
PCT/EP2008/005210 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène WO2009003634A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
BRPI0813945-8A2A BRPI0813945A2 (pt) 2007-06-29 2008-06-17 Processo para a conversão de cargas de alimentação pesadas a destilados.
CA2691794A CA2691794C (fr) 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogene
AP2010005119A AP2845A (en) 2007-06-29 2008-06-17 Process for the conversion of heavy hydrocarbon feedstocks to distillates with the self-production of hydrogen

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT001302A ITMI20071302A1 (it) 2007-06-29 2007-06-29 Procedimento per la conversione a distillati di cariche idrocarburiche pesanti con autoproduzione di idrogeno
ITMI2007A001302 2007-06-29

Publications (1)

Publication Number Publication Date
WO2009003634A1 true WO2009003634A1 (fr) 2009-01-08

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PCT/EP2008/005210 WO2009003634A1 (fr) 2007-06-29 2008-06-17 Processus de conversion de charges d'alimentation d'hydrocarbure lourdes en distillats avec auto production d'hydrogène

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Country Link
AP (1) AP2845A (fr)
BR (1) BRPI0813945A2 (fr)
CA (1) CA2691794C (fr)
IT (1) ITMI20071302A1 (fr)
WO (1) WO2009003634A1 (fr)

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CA2691794A1 (fr) 2009-01-08
CA2691794C (fr) 2016-04-12
AP2010005119A0 (en) 2010-02-28
ITMI20071302A1 (it) 2008-12-30
AP2845A (en) 2014-02-28
BRPI0813945A2 (pt) 2014-12-30

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