WO2006066857A1 - Procede de transformation de charges directes lourdes telles que des petroles bruts lourds et residus de distillation - Google Patents

Procede de transformation de charges directes lourdes telles que des petroles bruts lourds et residus de distillation Download PDF

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Publication number
WO2006066857A1
WO2006066857A1 PCT/EP2005/013684 EP2005013684W WO2006066857A1 WO 2006066857 A1 WO2006066857 A1 WO 2006066857A1 EP 2005013684 W EP2005013684 W EP 2005013684W WO 2006066857 A1 WO2006066857 A1 WO 2006066857A1
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Prior art keywords
process according
distillation
section
sda
heavy
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PCT/EP2005/013684
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English (en)
Inventor
Romolo Montanari
Mario Marchionna
Sergio Rosi
Nicoletta Panariti
Alberto Delbianco
Original Assignee
Eni S.P.A.
Snamprogetti S.P.A.
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Publication date
Application filed by Eni S.P.A., Snamprogetti S.P.A. filed Critical Eni S.P.A.
Priority to EP05819257A priority Critical patent/EP1838815A1/fr
Priority to CN200580046209.0A priority patent/CN101098949B/zh
Priority to AU2005318443A priority patent/AU2005318443B2/en
Priority to MX2007007545A priority patent/MX2007007545A/es
Priority to BRPI0519489A priority patent/BRPI0519489B1/pt
Publication of WO2006066857A1 publication Critical patent/WO2006066857A1/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
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1033—Oil well production fluids
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content
    • C10G2300/206—Asphaltenes
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/207—Acid gases, e.g. H2S, COS, SO2, HCN
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4081—Recycling aspects
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents

Definitions

  • PROCESS FOR THE CONVERSION OF HEAVY CHARGE STOCKS SUCH AS HEAVY CRUDE OILS AND DISTILLATION RESIDUES
  • the present invention relates to a process for the conversion of heavy charge stocks , among which heavy crude oils , bitumens from oil sands and distillation residues , by means of at least three process units : deasphalting, hydro- conversion of the charge stock using phase-dispersed catalysts and distillation.
  • the conversion of heavy crude oils , bitumens from oil sands and petroleum residues into liquid products can be substantially effected in two ways : an exclusively thermal one and the other by means of hydrogenating treatment .
  • the hydroconversion technologies which are at present on the market , use fixed or ebullated bed reactors and make use of catalysts generally consisting of one or more transition metals (Mo, W, Ni , Co, etc .. ) supported on silica/alumina (or equivalent material ) .
  • Fixed bed technologies have several problems in treating particularly heavy charge stocks , containing high percentages of hetero-atoms , metals and asphaltenes , as these contaminants lead to a fast deactivation of the catalyst .
  • Hydrotreating technologies using dispersed phase catalysts can represent an interesting solution to the drawbacks of the fixed and ebullated bed technologies .
  • Slurry processes in fact , combine the advantage of a high flexibility on the charge stock with high performances in terms of conversion and upgrading, proving, at least in principle , to be simpler from a technological point of view .
  • Slurry technologies are characterized by the presence of catalyst particles having very small average dimensions and suitably dispersed in the medium: for this reason the hydrogenation processes are easier and immediate in all parts of the reactor .
  • the formation of coke is considerably reduced and the upgrading of the charge stock is high .
  • the catalyst can be introduced as powder with suffi- ciently reduced dimensions (US- 4 , 303 , 634 ) or as an oil- soluble precursor (US-5 , 288 , 681) .
  • the active form of the catalyst generally the metal sulphide
  • the metal components of the dispersed catalysts are normally one or more transition metals (preferably Mo, W, Ni , Co or Ru) .
  • Molybdenum and tungsten have much more sat- isfactory performances with respect to nickel , cobalt or ruthenium, and even more with respect to vanadium and iron (N. Panariti et al . , Appl . Ctal . A: Gen . 2000 , 204 , 203 ) .
  • the way these catalysts are used are extremely important both from an economical and environmental point of view .
  • the catalyst can be used at a low concentration (a few hundred ppm) in the "once-through" mode , but in this case the upgrading of the reaction products is generally unsatisfactory (N . Pnariti et al . , Appl . Ctal . A: Gen . , 2000 , 204 , 203 and 215 ) .
  • the catalyst at the reactor outlet can be recovered by separation of the product obtained from the hydrotreating (preferably from the bottom of the distillation column downstream of the reactor) through conventional methods such as , for example , decanting, centrifugation or filtration (US-3 , 240 , 718 ; US-4 , 762 , 812 ) which are , however, ex- tremely complex if applied to heavy charge stocks rich in poisoning substances .
  • asphaltenes are hydrocarbons which can be precipitated from a crude oil or an oil residue , by treatment with a paraffinic hydrocarbon with a number of carbon atoms ranging from 3 to 7 , for example n-heptane un- der the standard conditions provided for by the regulation IP - 143 .
  • control of the loss of stability of a heavy charge stock during a thermal and/or catalytic conversion is therefore fundamental for obtaining the maximum conversion degree without creating problems due to the formation of coke or fouling .
  • the optimum operative conditions (mainly reaction temperature and residence time) are simply determined on the basis of the stability of the reactor effluent through direct measurements on the non- converted residue (P value , Hot Filtration Test , Spot Test , etc .. ) .
  • hydroconversion with catalysts in slurry phase (HT) , distillation or flash (D) , deasphalting (SDA) is characterized in that the three units operate on mixed streams consisting of fresh charge stock and recycled streams , using the following steps : * sending at least one fraction of the heavy charge stock to a deasphalting section (SDA) in the presence of solvents , obtaining two streams , one consisting of deasphalted oil (DAO) , the other of asphalts ; * mixing the asphalt with a suitable hydrogenation cata- lyst and possibly with the remaining fraction of the heavy charge stock not sent to the deasphalting section and sending the mix obtained to a hydrotreating reactor (HT) , introducing into the same reactor hydrogen or a mix of hydrogen and H 2 S; * sending the stream containing the product of the hy- drotreating reaction and the catalyst in dispersed phase to one or more distillation or flash (D)
  • n represents the number of carbon atoms of the paraffin used in the deasphalting operation (normally from 3 to 6) .
  • the process, obj ect of the present invention for the conversion of heavy and extra-heavy charge stocks by the combined use of at least the three following process units : solvent deasphalting (SDA) , hydroconversion with catalysts in slurry phase (HT) , distillation or flash (D) , is characterized in that it comprises the following steps :
  • the heavy charge stocks treated can be of a varying nature : they can be selected from heavy crude oils , distillation residues , heavy oils coming from catalytic treatments , for example “unconverted oils” from fixed or ebul- lated bed hydrotreatment , “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 other high boiling charge stock of a hydrocarbon origin, normally known in the art as “black oils” .
  • the stream containing asphaltenes obtained in the deasphalting section (SDA) can be optionally mixed with the remaining part of the distillation residue (tar) , or the liquid coming from the flash unit , not recycled to the hy- drotreatment section (HT) .
  • Said stream containing asphaltenes , mixed or not mixed with part of the distillation residue (tar) or of the liquid coming from the flash unit can be :
  • the gasification can be effected by feeding to the gasification unit , in addition to the charge stock, oxygen and vapour which react under exothermic conditions at a temperature of over 1300 0 C and a pressure ranging from 30 to 80 bar, to produce mainly H 2 and CO .
  • a stream of syngas , or a mix of H 2 and CO, can be obtained from the gasification section, which can be further used as fuel by means of combustion with combined cycles (IGCC) or transformed into paraffinic hydrocarbons by means of Fisher-Tropsch synthesis or converted into methanol , dimethyl ether, formaldehyde and, more generally, into the whole series of products deriving from Cl chemistry .
  • IGCC combustion with combined cycles
  • the same paraffinic hydrocarbons obtained via Fisher- Tropsch can be mixed with the various cuts obtained from the distillation or flash step , improving their composition characteristics .
  • the catalyst precursors used can be selected from those obtained 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 catalyst concentration defined on the basis of the concentration of the metal or metals present in the hy- droconversion reactor, ranges from 350 to 30 , 000 ppm, preferably from 3 , 000 to 20 , 000 ppm, more preferably from 5 , 000 to 15 , 000 ppm.
  • the hydrotreatment step (HT) is preferably carried out at a temperature ranging from 360 to 450 0 C, more preferably from 380 to 440 0 C, and at a pressure ranging from 3 to 30 MPa, preferably from 10 to 20 MPa .
  • Hydrogen is fed to the reactor, which can operate in both a down-flow mode and, preferably, up-flow. Said gas can be fed to several sections of the reactor .
  • the distillation steps are preferably effected under reduced pressure , ranging from 0.001 to 0.5 MPa, preferably from 0.1 to 0.3 MPa .
  • the hydrotreatment step (HT) can consist of one or more reactors operating within the condition range mentioned above . Part of the distillates produced in the first reactor can be recycled to the subsequent reactors of the same step .
  • the deasphalting step (SDA) effected by means of an extraction with solvent , either a hydrocarbon solvent or not , is normally carried out at temperatures ranging from 40 to 200 0 C and a pressure of 0.1 to 7 MPa .
  • the solvent recovery can be effected under sub-critical or supercritical multi-step conditions , thus allowing a further fractionation between the 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 , more preferably having 5 carbon atoms .
  • a further secondary section can be optionally present for the hydro- genation post-treatment of the C 2 -500 °C fraction, pref- erably the C 5 -350 °C fraction, coming from the section of high pressure separators envisaged upstream of the distillation .
  • the stream containing the hydro- treatment reaction product and the catalyst in dispersed phase is subj ected to a separation pre-step, effected at high pressure , so as to obtain a light fraction and a heavy fraction, this heavy fraction alone being sent to said distillation (D) step (s) .
  • the light fraction obtained from the high pressure separation step can be sent to a hydrotreatment section, producing a lighter fraction containing Ci-C 4 and H 2 S gas and a less light fraction containing hydrotreated naphtha and gas oil .
  • fuels can be obtained, starting from oil charge stocks which are extremely rich in sulphur, in line with the strictest specifications on the sulphur content ( ⁇ 10-50 ppm of sulphur) and improved as far as other characteristics of diesel gas oil are concerned, such as density, poly-aromatic hydrocarbon content and the cetane number;
  • the post-treatment hydrogenation on a fixed bed consists of the preliminary separation of the reaction effluent of the hydrotreatment reactor (HT) by means of one or more separators operating at high pressure and high temperature .
  • the heavy part extracted from the bottom, is sent to the main distillation unit , the aliquot which is extracted from the head, a C 5 -350 °C fraction, is sent to a secondary treatment section in the presence of hydrogen, available at high pressure , where the reactor is of the fixed bed type and contains a typical desulphurisa- tion/dearomatisation catalyst , in order to obtain a product which having a considerably lowered sulphur content and also lower nitrogen contents , a lower total density and, at the same time, increased cetane numbers as far as the gas oil fraction is concerned .
  • the hydrotreatment section normally consists of one or more reactors in series ; , the product of this system can be subsequently further fractionated by distillation to obtain a thoroughly desulphurated naphtha and a diesel gas oil within specification as fuel .
  • the fixed-bed hydrodesulphurisation step normally uses typical fixed-bed catalysts for gas oil hydrodesulphurisation; said catalyst , or possibly a mix of catalysts or a series of reactors with various catalysts having different properties , causes a deep refining of the light fraction, significantly reducing the sulphur and nitrogen content , increasing the hydrogenation degree of the charge stock, thus diminishing the density and increasing the cetane number of the gas oil fraction, at the same time reducing the formation of coke .
  • the catalyst normally consists of an amorphous part based on alumina, silica, silico-alumina and blends of different mineral oxides , on which a hydrodesulphurizing component in association with a hydrogenating product , is deposited (with several methods) .
  • Catalysts based on molybde- nura or tungsten with the addition of nickel and/or cobalt , deposited on a mineral amorphous carrier, are typical catalysts for this type of operation .
  • the post-treatment hydrogenation reaction is effected at an absolute pressure slightly lower than that of the pri- mary hydrotreatment step, normally ranging from 7 to 14
  • the space velocity is another im- portant variable in controlling the quality of the product obtained : it can range from 0.1 to 5 h "1 , preferably from
  • the quantity of hydrogen mixed with the charge stock is fed at a flow-rate ranging from 100 to 5 , 000 Nm 3 /m 3 , pref- erably from 300 to 1 , 000 Nm 3 /m 3 .
  • Two streams are obtained from the deasphalting unit (SDA) : one stream (2 ) consisting of deasphalted oil (DAO) , the other stream containing asphaltenes (3 ) .
  • the stream containing asphaltenes (3 ) is sent to a gasi- fication section (PO x ) in order to obtain syngas, i . e . a gaseous mix of H 2 and CO (4 ) .
  • the stream consisting of deasphalted oil (2 ) is mixed with the fresh make-up catalyst (5) (necessary for reinte- grating that lost with the stream (15 ) described hereunder) and with the stream ( 14) (described hereunder) coming from the bottom of the distillation or flash column (D) to form the stream (6) which is fed to the hydrotreatment reactor (HT) into which hydrogen (or a mix containing hydrogen and H 2 S) (7) is fed .
  • HT hydrotreatment reactor
  • the hydrogen fed can be part of the hydrogen coming from the gasification step (PO x ) (not schematised in the figure) .
  • a stream (8) leaves the reactor (HT) , containing the hy- drogenation product and the catalyst in dispersed phase , which is fractionated in a distillation or flash column (D) from which the lighter fraction (9) separates together with the distillable products (10 ) , (11) and (12 ) from the distillation residue (13 ) containing the dispersed catalyst and coke .
  • This stream (13 ) (called tar) is mostly recycled (14 ) to the hydrotreatment unit (HT) , the remaining part (15) being sent to the gasification section (PO x ) .
  • Example 1 An example is provided for a better understanding of the invention, it being understood that the invention should not be considered as being limited thereto or thereby .
  • Example 1
  • the yield obtained by the procedure described is equal to 82% by weight of deasphalted oil with respect to the starting vacuum residue .
  • RV Ural and deasphalted oil are shown in table 1.
  • Table 1 Characteristics of the vacuum residue Ural 500 0 C and DAO n-C5 extracted .
  • Catalytic tests were carried out using a stirred micro-autoclave of 30 cm 3 , in accordance with the following general operative procedure : about 10 g of the charge stock are introduced into the reactor and the catalyst precursor is added; the system is then pressurized with hydrogen and brought to temperature by means of an electrically heated oven; the system is maintained under stirring during the reaction by a swinging capillary system operating at a rotational rate of 900 rpm; moreover, the total pressure is kept constant by means of an automatic reintegration system of the hydrogen consumed; - quenching of the reaction is carried out once the test has been completed; the autoclave is then de- pressurised and the gas collected in a sampling bag; the gaseous samples are then sent for gas- chromatographic analysis ; - the products present in the reactor are recovered without the addition of any solvent , and analyzed in terms of distribution of the distillates , sulphur content , nitrogen content , coal residue and metal content .
  • Atmospheric gas oil (AGO, 170-350 0 C) : 27%
  • Vacuum gas oil (VGO, 350 -500 0 C) : 31%

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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)
  • Catalysts (AREA)
  • Working-Up Tar And Pitch (AREA)

Abstract

L’invention concerne un procédé de transformation de charges directes lourdes utilisant en combinaison au moins les trois unités de traitement suivantes: désasphaltage par solvant (SDA), hydroconversion à catalyseurs en phase de suspension (HT), distillation ou détente brusque (D). Le procédé est caractérisé en ce qu'il comporte les étapes suivantes: amener la charge directe lourde vers la partie désasphaltage (SDA); mélanger le flux constitué de pétrole désasphalté (DAO) avec un précurseur de catalyseur d'hydrogénation approprié et amener le mélange obtenu vers un réacteur d'hydrotraitement (HT); soumettre le flux contenant le produit de la réaction d'hydrotraitement et le catalyseur en phase dispersée à une ou à plusieurs étapes de distillation ou de détente brusque (D); recycler au moins une partie du résidu de distillation (goudron) ou le liquide provenant de l'unité de détente brusque.
PCT/EP2005/013684 2004-12-22 2005-12-19 Procede de transformation de charges directes lourdes telles que des petroles bruts lourds et residus de distillation WO2006066857A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP05819257A EP1838815A1 (fr) 2004-12-22 2005-12-19 Procede de transformation de charges directes lourdes telles que des petroles bruts lourds et residus de distillation
CN200580046209.0A CN101098949B (zh) 2004-12-22 2005-12-19 用于重质原料例如重质原油和蒸馏渣油转化的方法
AU2005318443A AU2005318443B2 (en) 2004-12-22 2005-12-19 Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residues
MX2007007545A MX2007007545A (es) 2004-12-22 2005-12-19 Proceso para la conversion de materias primas de carga pesada como petroleos crudos pesados y residuos de destilacion.
BRPI0519489A BRPI0519489B1 (pt) 2004-12-22 2005-12-19 processo para a conversão de matérias-primas de carga pesada

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT002446A ITMI20042446A1 (it) 2004-12-22 2004-12-22 Procedimento per la conversione di cariche pesantyi quali i greggi pesanti e i residui di distillazione
ITMI2004A002446 2004-12-22

Publications (1)

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WO2006066857A1 true WO2006066857A1 (fr) 2006-06-29

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PCT/EP2005/013684 WO2006066857A1 (fr) 2004-12-22 2005-12-19 Procede de transformation de charges directes lourdes telles que des petroles bruts lourds et residus de distillation

Country Status (9)

Country Link
US (2) US20060272982A1 (fr)
EP (1) EP1838815A1 (fr)
CN (1) CN101098949B (fr)
AU (1) AU2005318443B2 (fr)
BR (1) BRPI0519489B1 (fr)
CA (1) CA2530906C (fr)
IT (1) ITMI20042446A1 (fr)
MX (1) MX2007007545A (fr)
WO (1) WO2006066857A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008027131A1 (fr) * 2006-08-31 2008-03-06 Exxonmobil Chemical Patents Inc. Disposition de goudron de vapocraquage
US8083930B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. VPS tar separation
US8083931B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. Upgrading of tar using POX/coker
WO2013184462A1 (fr) * 2012-06-05 2013-12-12 Saudi Arabian Oil Company Procédé intégré de désasphaltage et de désulfurisation de pétrole brut total

Families Citing this family (63)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITMI20011438A1 (it) * 2001-07-06 2003-01-06 Snam Progetti Procedimento per la conversione di cariche pesanti quali i graggi pesanti e i residui di distillazione
US7678732B2 (en) 2004-09-10 2010-03-16 Chevron Usa Inc. Highly active slurry catalyst composition
US7972499B2 (en) 2004-09-10 2011-07-05 Chevron U.S.A. Inc. Process for recycling an active slurry catalyst composition in heavy oil upgrading
CN1325605C (zh) * 2005-12-07 2007-07-11 中国海洋石油总公司 一种油砂沥青的处理方法
US7938954B2 (en) 2005-12-16 2011-05-10 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US8435400B2 (en) 2005-12-16 2013-05-07 Chevron U.S.A. Systems and methods for producing a crude product
US8372266B2 (en) 2005-12-16 2013-02-12 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US7943036B2 (en) 2009-07-21 2011-05-17 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US7931796B2 (en) 2008-09-18 2011-04-26 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US8048292B2 (en) 2005-12-16 2011-11-01 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US7431822B2 (en) 2005-12-16 2008-10-07 Chevron U.S.A. Inc. Process for upgrading heavy oil using a reactor with a novel reactor separation system
ITMI20061512A1 (it) * 2006-07-31 2008-02-01 Eni Spa Procedimento per la conversione totale di cariche pesanti a distillati
ITMI20061511A1 (it) * 2006-07-31 2008-02-01 Eni Spa Procedimento per la conversione totale a distillati di cariche pesanti
US7674369B2 (en) * 2006-12-29 2010-03-09 Chevron U.S.A. Inc. Process for recovering ultrafine solids from a hydrocarbon liquid
ITMI20071303A1 (it) * 2007-06-29 2008-12-30 Eni Spa Procedimento per la conversione di cariche idrocarburiche pesanti a distillati con autoproduzione di idrogeno
US8221710B2 (en) * 2007-11-28 2012-07-17 Sherritt International Corporation Recovering metals from complex metal sulfides
US7964090B2 (en) * 2008-05-28 2011-06-21 Kellogg Brown & Root Llc Integrated solvent deasphalting and gasification
US7931797B2 (en) * 2009-07-21 2011-04-26 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US7897036B2 (en) 2008-09-18 2011-03-01 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US7897035B2 (en) 2008-09-18 2011-03-01 Chevron U.S.A. Inc. Systems and methods for producing a crude product
US8236169B2 (en) 2009-07-21 2012-08-07 Chevron U.S.A. Inc Systems and methods for producing a crude product
US7935243B2 (en) 2008-09-18 2011-05-03 Chevron U.S.A. Inc. Systems and methods for producing a crude product
CA2683123C (fr) * 2008-10-22 2016-08-09 Total E&P Canada Ltd. Procede et systeme de production de sous-produits asphaltenes dans des installations de traitement de mousse paraffinique
US20100122934A1 (en) * 2008-11-15 2010-05-20 Haizmann Robert S Integrated Solvent Deasphalting and Slurry Hydrocracking Process
AU2010229809B2 (en) * 2009-03-25 2015-02-12 Chevron U.S.A. Inc. Process for recovering metals from coal liquefaction residue containing spent catalysts
US8927448B2 (en) 2009-07-21 2015-01-06 Chevron U.S.A. Inc. Hydroprocessing catalysts and methods for making thereof
US8759242B2 (en) 2009-07-21 2014-06-24 Chevron U.S.A. Inc. Hydroprocessing catalysts and methods for making thereof
US9068132B2 (en) 2009-07-21 2015-06-30 Chevron U.S.A. Inc. Hydroprocessing catalysts and methods for making thereof
US8882991B2 (en) * 2009-08-21 2014-11-11 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking high boiling point hydrocarbon feedstock
FR2958658B1 (fr) * 2010-04-13 2012-03-30 Inst Francais Du Petrole Procede d'hydroconversion de charges petrolieres via une technologie en slurry permettant la recuperation des metaux du catalyseur et de la charge mettant en oeuvre une etape de lixiviation.
FR2958656B1 (fr) * 2010-04-13 2012-05-11 Inst Francais Du Petrole Procede d'hydroconversion de charges petrolieres via une technologie en slurry permettant la recuperation des metaux du catalyseur et de la charge mettant en oeuvre une etape d'extraction.
US9481835B2 (en) * 2010-03-02 2016-11-01 Meg Energy Corp. Optimal asphaltene conversion and removal for heavy hydrocarbons
GB2478332A (en) 2010-03-04 2011-09-07 Grimley Smith Associates Method of metals recovery from refinery residues
WO2012092006A2 (fr) 2010-12-30 2012-07-05 Chevron U.S.A. Inc. Catalyseurs d'hydrotraitement et leurs procédés de fabrication
KR20140034145A (ko) * 2011-02-11 2014-03-19 릴라이언스 인더스트리즈 리미티드 중질 방향족 탄화수소의 방향족성을 개선하기 위한 공정
WO2013015883A1 (fr) 2011-07-27 2013-01-31 Saudi Arabian Oil Company Production de gaz de synthèse à partir de résidus de procédé de désasphaltage par solvant dans un réacteur de gazéification à paroi membranaire
US9150794B2 (en) 2011-09-30 2015-10-06 Meg Energy Corp. Solvent de-asphalting with cyclonic separation
US9200211B2 (en) 2012-01-17 2015-12-01 Meg Energy Corp. Low complexity, high yield conversion of heavy hydrocarbons
CN103242894A (zh) * 2012-06-18 2013-08-14 上海河图工程股份有限公司 一种不需外供氢源的重油浆态床加氢组合工艺
US9687823B2 (en) 2012-12-14 2017-06-27 Chevron U.S.A. Inc. Hydroprocessing co-catalyst compositions and methods of introduction thereof into hydroprocessing units
US9321037B2 (en) 2012-12-14 2016-04-26 Chevron U.S.A., Inc. Hydroprocessing co-catalyst compositions and methods of introduction thereof into hydroprocessing units
JP6609478B2 (ja) 2013-02-25 2019-11-20 エムイージー エナジー コーポレイション 新規な装置及び方法（「ｉａｓ」）を使用する重液炭化水素からの固体アスファルテンの改良型分離
US9650312B2 (en) 2013-03-14 2017-05-16 Lummus Technology Inc. Integration of residue hydrocracking and hydrotreating
US9677015B2 (en) 2013-06-20 2017-06-13 Exxonmobil Research And Engineering Company Staged solvent assisted hydroprocessing and resid hydroconversion
WO2014205169A1 (fr) 2013-06-20 2014-12-24 Exxonmobil Research And Engineering Company Hydroconversion séquentielle de bouillie de pétrole brut lourd
WO2014205178A1 (fr) 2013-06-20 2014-12-24 Exxonmobil Research And Engineering Comapny Hydroconversion de boues et cokéfaction d'huiles lourdes
WO2014205185A1 (fr) 2013-06-20 2014-12-24 Exxonmobil Research And Engineering Company Hydroconversion de suspension épaisse à l'aide de catalyseurs de suspension épaisse améliorés
US9605218B2 (en) 2013-06-20 2017-03-28 Exxonmobil Research And Engineering Company Integrated hydrocracking and slurry hydroconversion of heavy oils
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US9783748B2 (en) 2014-09-09 2017-10-10 Uop Llc Process for producing diesel fuel
US9663732B2 (en) 2014-09-09 2017-05-30 Uop Llc Process for controlling operations of a residue process unit
US9849446B2 (en) 2015-08-21 2017-12-26 Exxonmobil Research And Engineering Company Slurry hydroconversion catalysts
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ES2925285T3 (es) * 2018-09-25 2022-10-14 Eni Spa Procedimiento para la hidroconversión de productos petroleros pesados con reciclaje
CA3131283A1 (fr) * 2019-03-04 2020-09-10 China Petroleum & Chemical Corporation Procede et systeme de production d'olefine legere a partir d'une huile pauvre
CN111647432B (zh) * 2019-03-04 2021-08-06 中国石油化工股份有限公司 一种由低品质油生产低碳烯烃的改质方法和系统
US20240018433A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex
US11939541B2 (en) 2022-07-15 2024-03-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex
US20240018432A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit, steam enhanced catalytic cracker, and an aromatics complex
US11851622B1 (en) * 2022-07-15 2023-12-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit and steam enhanced catalytic cracker

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2004035A1 (de) * 1968-01-25 1971-08-05 Exxon Research Engineering Co Krackverfahren
US4126538A (en) * 1976-09-22 1978-11-21 Shell Oil Company Process for the conversion of hydrocarbons
GB1546960A (en) * 1975-10-15 1979-05-31 Shell Int Research Process for the conversion of hydrocarbons
US4431510A (en) * 1982-04-01 1984-02-14 Uop Inc. Process for producing hydrogen-enriched hydrocarbonaceous products from coal
EP0309621A1 (fr) * 1987-09-28 1989-04-05 Uop Contrôle des sous-produits aromatiques polynucléaires dans un procédé d'hydrocraquage

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3663429A (en) * 1970-04-09 1972-05-16 Atlantic Richfield Co Process for hydroconversion of raw shale oil
NL7507484A (nl) * 1975-06-23 1976-12-27 Shell Int Research Werkwijze voor het omzetten van koolwaterstoffen.
US4424110A (en) * 1980-08-29 1984-01-03 Exxon Research And Engineering Co. Hydroconversion process
US4428824A (en) * 1982-09-27 1984-01-31 Mobil Oil Corporation Process for visbreaking resid deasphaltenes
US4534854A (en) * 1983-08-17 1985-08-13 Exxon Research And Engineering Co. Delayed coking with solvent separation of recycle oil
US5024570A (en) * 1988-09-14 1991-06-18 Fujitsu Limited Continuous semiconductor substrate processing system
US5024750A (en) * 1989-12-26 1991-06-18 Phillips Petroleum Company Process for converting heavy hydrocarbon oil
US5935423A (en) * 1997-04-12 1999-08-10 Atlantic Richfield Company Method for producing from a subterranean formation via a wellbore, transporting and converting a heavy crude oil into a distillate product stream
US5958365A (en) * 1998-06-25 1999-09-28 Atlantic Richfield Company Method of producing hydrogen from heavy crude oil using solvent deasphalting and partial oxidation methods
ATE277146T1 (de) * 1998-07-29 2004-10-15 Texaco Development Corp Integriertes lösungsmittelentasphaltierungs- und vergasungsverfahren
DE60006783T2 (de) * 1999-01-11 2004-09-30 Texaco Development Corp. Integriertes lösungsmittelentasphaltierungs- , vergasungs- und wasserstoffbehandlungsverfahren
US6444116B1 (en) * 2000-10-10 2002-09-03 Intevep, S.A. Process scheme for sequentially hydrotreating-hydrocracking diesel and vacuum gas oil
ITMI20011438A1 (it) * 2001-07-06 2003-01-06 Snam Progetti Procedimento per la conversione di cariche pesanti quali i graggi pesanti e i residui di distillazione
CA2510357C (fr) * 2002-12-20 2012-09-25 Eni S.P.A. Procede pour la conversion de charges lourdes telles que des huiles brutes lourdes et des residus de distillation

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2004035A1 (de) * 1968-01-25 1971-08-05 Exxon Research Engineering Co Krackverfahren
GB1305932A (fr) * 1968-01-25 1973-02-07
GB1546960A (en) * 1975-10-15 1979-05-31 Shell Int Research Process for the conversion of hydrocarbons
US4126538A (en) * 1976-09-22 1978-11-21 Shell Oil Company Process for the conversion of hydrocarbons
US4431510A (en) * 1982-04-01 1984-02-14 Uop Inc. Process for producing hydrogen-enriched hydrocarbonaceous products from coal
EP0309621A1 (fr) * 1987-09-28 1989-04-05 Uop Contrôle des sous-produits aromatiques polynucléaires dans un procédé d'hydrocraquage

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP1838815A1 *

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008027131A1 (fr) * 2006-08-31 2008-03-06 Exxonmobil Chemical Patents Inc. Disposition de goudron de vapocraquage
US8083930B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. VPS tar separation
US8083931B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. Upgrading of tar using POX/coker
US8709233B2 (en) 2006-08-31 2014-04-29 Exxonmobil Chemical Patents Inc. Disposition of steam cracked tar
WO2013184462A1 (fr) * 2012-06-05 2013-12-12 Saudi Arabian Oil Company Procédé intégré de désasphaltage et de désulfurisation de pétrole brut total
CN104540926A (zh) * 2012-06-05 2015-04-22 沙特阿拉伯石油公司 用于全原油脱沥青和脱硫的集成式工艺

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AU2005318443B2 (en) 2011-01-20
US20130112593A1 (en) 2013-05-09
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US20060272982A1 (en) 2006-12-07
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