EP0113283B1 - Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères - Google Patents

Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères Download PDF

Info

Publication number
EP0113283B1
EP0113283B1 EP83402494A EP83402494A EP0113283B1 EP 0113283 B1 EP0113283 B1 EP 0113283B1 EP 83402494 A EP83402494 A EP 83402494A EP 83402494 A EP83402494 A EP 83402494A EP 0113283 B1 EP0113283 B1 EP 0113283B1
Authority
EP
European Patent Office
Prior art keywords
catalyst
pores
pore volume
nanometers
alumina
Prior art date
Legal status (The legal status 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 status listed.)
Expired
Application number
EP83402494A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0113283A1 (fr
Inventor
Alain Billon
Yves Jacquin
Jean-Pierre Peries
Hervé Toulhoat
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
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 IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Publication of EP0113283A1 publication Critical patent/EP0113283A1/fr
Application granted granted Critical
Publication of EP0113283B1 publication Critical patent/EP0113283B1/fr
Expired legal-status Critical Current

Links

Images

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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing 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
    • 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

Definitions

  • the invention relates to the treatment of heavy oils or heavy petroleum fractions, with a high asphaltene content, with the aim of converting them into lighter, more easily transportable or processable fractions by the usual refining processes.
  • Coal hydrogenation oils can also be processed.
  • the invention solves the problem of the transformation of a viscous crude oil, non-transportable, rich in metals, sulfur and asphaltenes, and containing more than 50% of constituents with a normal boiling point above 520 ° C., into a stable hydrocarbon product, easily transportable, of low content of metals, sulfur and asphaltenes and having only a reduced content, for example less than 20% by weight, of constituents with a normal boiling point above 520 ° C. .
  • the problem solved by the invention has long been the subject of work; the main difficulty to be overcome is that of deactivation of the catalysts by impurities, in particular metallic impurities, of the treated charges.
  • impurities in particular metallic impurities
  • crude oil from Boscan or Cerro Negro can contain 200 to 1000 ppm by weight, or more, of metals; these metals are mainly vanadium and nickel, with varying proportions of iron and other metals.
  • the catalyst of step (a) is a catalyst which does not adsorb asphaltenes and metals (column 3, lines 19 to 21).
  • EP-A-55 164 relates to alumina agglomerates of particular characteristics and a method of preparation of these agglomerates. This document further reveals that these agglomerates can be used as a support for the manufacture of catalysts which can be used in a very large number of reactions. Among the reactions for which this support can be used are hydrotreatments of petroleum products (page 11, lines 21 to 32).
  • the supports prepared according to the process described in this document can be microporous, macroporous or be of bimodal type, that is to say, comprising micropores and macropores.
  • the majority of the supports described in the examples are of bimodal type comprising both macropores and micropores.
  • the weight ratio of catalyst C 2 to catalyst Ci is preferably from 1: 1 to 9: 1.
  • step (a) has been described in French patent application 82 10757 of June 17, 1982 and in patent application EP-A 98 764. The essential information is given below.
  • a large proportion, most often at least 50% of the acicular platelets have a dimension along their axis of greatest development of between 0.05 micrometers and preferably between 0.1 and 2 micrometers, a ratio of this dimension at their average width between 2 and 20, and preferably between 5 and 15, a ratio of this dimension to their average thickness between 1 and 5000, and preferably between 10 and 200.
  • a large proportion, most often at at least 50% of the acicular platelet agglomerates constitute a collection of pseudo-spherical particles of average size between 1 and 20 micrometers, preferably between 2 and 10 micrometers. Very suitable images to represent such a structure are for example a bunch of thorny chestnut bugs, or a bunch of sea urchins.
  • FIG. 1 makes it possible to compare the porous distribution curve of a catalyst (A) as used in step (a) of the invention and those corresponding to monomodal (C) or bimodal (B) catalysts produced according to prior art.
  • the specific surface of this catalyst is between 50 and 250 m 2 / g and particularly preferably between 120 and 180 m 2 / g.
  • FIG. 2 to 5 show four micrographs at 300 times, 3000 times, 10,000 times and 20,000 times respectively of a catalyst used according to the invention (catalyst A) which illustrate the particular structure in juxtaposed sea urchins that are just described.
  • FIG. 6 presents a photomicrograph with a nominal magnification of 110,000 times of a bundle of needle-shaped plates of catalyst A, which clearly illustrates the typical appearance of these plates.
  • the intervals between the opposite arrows marked 1 mark the trace of platelets on the field and are an approximate measure of the thickness of these platelets.
  • the interval between the opposite arrows marked 2 marks a plate parallel to the plane of the photograph and is a measure of the average width of this plate.
  • the scale is 9 nanometers per millimeter and the dark parts correspond to the catalytic material.
  • FIGS. 7 to 10 show four microphotographs taken at the same respective magnifications as FIGS. 2 to 5 and with the same apparatus, on a sample of catalyst (catayleur B) prepared using bimodal alumina beads obtained by the process patented in France under the number 2 449 474: these photographs illustrate well the description which is given in this last patent, namely that the macroporosity results from the interparticle voids existing between microporous spheroidal particles, of which the particle size distribution and the compactness of the stacking determine the macroporous volume and the size of the macropores.
  • FIGS. 7 to 10 show four microphotographs taken at the same respective magnifications as FIGS. 2 to 5 and with the same apparatus, on a sample of catalyst (catayleur B) prepared using bimodal alumina beads obtained by the process patented in France under the number 2 449 474: these photographs illustrate well the description which is given in this last patent, namely that the macroporosity results from the interparticle void
  • the dark areas correspond to the empty spaces of the structures of the catalysts, that is to say to the macroporosity, while the light parts correspond to the catalytic material.
  • the distribution of the diameters of the macropores of catalyst B can be measured in the photographs and it corresponds well to that obtained by porosimetry with mercury and which is represented in FIG. 1.
  • the comparison of the microphotographs clearly shows that the spheroidal particles microporous catalyst B do not have the sea urchin structure obtained for catalyst A used in step (a) of the invention.
  • a catalyst which can be used for stage (a) of the invention can be prepared according to the following method, without limiting the invention to this particular method of preparation: Use is made, as support, of alumina agglomerates in particles of the order of 0.1 to 10 millimeters or powder in particles of the order of 20 to 100 micrometers themselves having the above-mentioned sea urchin structure and having substantially the same characteristics as those of the catalyst of the invention, no. particularly with regard to the shapes and dimensions of the wafers and agglomerates, the specific surface and the porosity.
  • the catalytic metal or metals namely at least one metal or metal compound belonging to at least one of groups V, VI and VIII (iron group) of the classification periodic, more particularly at least one of the following metals: molybdenum, tungsten, iron, vanadium, cobalt and nickel.
  • molybdenum + cobalt molybdenum + nickel, vanadium + nickel, tungsten + nickel.
  • the aforementioned metals are most often introduced in the form of precursors such as oxides, acids, salts, organic complexes, and in amounts such that the catalyst contains from 0.5 to 40% and preferably from 1 to 20% by weight of these metals expressed as oxides. These precursors are well known and it is therefore unnecessary to list them here. We finish with optional drying and heat treatment at a temperature between 400 and 800 degrees centigrade.
  • the active alumina agglomerates used according to the present invention can be prepared from an active alumina powder having a poorly crystallized and / or amorphous structure, for example obtained according to the process described in; French patent n ° 1,438,497.
  • the active alumina used is generally obtained by rapid dehydration of aluminum hydroxides such as bayerite, hydrargillite or gibbsite, nordstrandite or aluminum oxyhydroxides such as boehmite and diaspore.
  • the agglomeration of alumina is carried out according to methods well known to those skilled in the art and, in particular, by pelleting, extrusion, bead shaping with a rotating bezel, etc.
  • this agglomeration is carried out, as is well known to those skilled in the art, by adding blowing agents to the mixture to be agglomerated.
  • blowing agents which can be used are in particular wood flour, charcoal, cellulose, starches, naphthalene, and, in general, all the organic compounds capable of being eliminated by calcination.
  • the active alumina agglomerates obtained generally have the following characteristics: their loss on ignition measured by calcination at 1000 ° C. is between approximately 1 and approximately 15%, their specific surface is between approximately 100 and approximately 350 m 2 / g, their total pore volume is between approximately 0.45 and approximately 1.5 c m 3 / g.
  • the active alumina agglomerates are then treated in an aqueous medium consisting of a mixture of at least one acid making it possible to dissolve at least part of the alumina of the agglomerates and at least one compound providing an anion capable of forming combine with aluminum ions in solution.
  • the term “acid making it possible to dissolve at least part of the alumina of the agglomerates” means any acid which, brought into contact with the active alumina agglomerates defined above, achieves the dissolution of at least part of the aluminum ions.
  • the acid must dissolve at least 0.5% and at most 15% by weight of alumina in the agglomerates. Its concentration in the aqueous treatment medium must be less than 20% by weight and preferably between 1% and 15%.
  • Use will preferably be made of strong acids such as nitric acid, hydrochloric acid, perchloric acid, sulfuric acid or weak acids used at a concentration such that their aqueous solution has a pH of less than about 4 .
  • the term “compound providing an anion capable of combining with the aluminum ions in solution” is understood to mean any compound capable of liberating an anion A (-n) capable of forming with the cations AI (3+) products in which the atomic ratio n (A / Al) is less than or equal to 3.
  • a particular case of these compounds can be illustrated by the basic salts of general formula A12 (OH)., Ay in which 0 ⁇ x ⁇ 6; ny ⁇ 6; n represents the number of charges of anion A.
  • the concentration of this compound in the aqueous treatment medium must be less than 50% by weight and preferably between 3% and 30%.
  • Use is preferably made of the compounds capable of releasing in solution the anions chosen from the group consisting of the nitrate, chloride, sulfate, perchlorate, chloroacetate, dichloracetate, trichloracetate, bromoacetate, dibromacetate anions, and the anions of general formula: in which R represents a radical taken from the group comprising H, CH 3 , C 2 H 5 , CH 3 CH 2 CH 2 , (CH 3 ) 2 CH.
  • the compounds capable of liberating the anion A (-n) in solution can operate this liberation, either directly for example by dissociation, or indirectly for example by hydrolysis.
  • the compounds can in particular be chosen from the group comprising: mineral or organic acids, anhydrides, organic or mineral salts, esters.
  • mineral salts there may be mentioned the alkaline or alkaline-earth salts soluble in an aqueous medium, such as those of sodium, potassium, magnesium or calcium, ammonium salts, aluminum salts, earth salts rare.
  • This treatment can be carried out either by dry impregnation of the agglomerates, or by immersion of the agglomerates in the aqueous solution consisting of the above-mentioned mixture of acid and of compound providing the desired anion.
  • dry impregnation is intended to bring the alumina agglomerates into contact with a volume of solution less than or equal to the total pore volume of the agglomerates treated.
  • mixtures of nitric and acetic acid or nitric and formic acid will be used as the aqueous medium.
  • the agglomerates thus treated are subjected simultaneously or subsequently to a treatment at a temperature between approximately 80 and approximately 250 ° C. for a period of time between approximately 5 minutes and approximately 36 hours.
  • This hydrothermal treatment does not cause any loss of alumina.
  • the operation is preferably carried out at a temperature between 120 and 220 ° C. for a period of time between 15 minutes and 18 hours.
  • This treatment constitutes a hydrothermal treatment of the active alumina agglomerates which realizes the transformation of at least part of these into boehmite.
  • This hydrothermal treatment can be carried out either under saturated vapor pressure, or under a partial vapor pressure of water at least equal to 70% of the saturated vapor pressure corresponding to the treatment temperature.
  • the concentration of the acid and of the compound in the treatment mixture and the hydrothermal treatment conditions used are such that there is no loss of alumina.
  • the increase in porosity following the treatment is therefore due to an expansion of the agglomerates during the treatment and not to a loss of alumina.
  • the agglomerates thus treated are then optionally dried at a temperature generally between approximately 100 and 200 ° C. for a period of time sufficient to remove the water which is not chemically bound.
  • the agglomerates are then subjected to thermal activation at a temperature between about 500 ° C and about 1100 ° C for a period between about 15 minutes and 24 hours.
  • Activation operations can be done in several stages. Activation is preferably carried out at a temperature between about 550 ° C and 950 ° C.
  • VPT total pore volume
  • the aforementioned process for the preparation of alumina agglomerates makes it possible in particular and completely unexpectedly to modify the distribution of the pore volumes according to the pore size of the untreated agglomerates. It makes it possible in particular to increase the proportion of pores between 10 and 100 nanometers, to reduce the proportion of pores less than 10 nanometers and to decrease the proportion of pores greater than 500 nanometers by modifying little the proportion of pores between 100 and 500 nanometers.
  • the alumina agglomerates thus obtained may have been thermally stabilized by rare earths, silica or alkaline earth metals.
  • step (c) of the process it has been specified above that the operation is preferably carried out using two successive beds of catalysts, named above (Ci) and (C 2 ).
  • the catalyst support (C,) preferably consists of an alumina of low acidity, that is to say having a heat of neutralization by adsorption of ammonia at 320 ° C less than 40 joules (and preferably less than 30 joules) per gram of alumina, under an ammonia pressure of 0.4 bars.
  • This alumina support has an area of 50 to 300 m 2 / g and preferably 40 to 150 m 2 / g, as well as a pore volume generally between 0.4 and 1.3 cm 3 / g .
  • the aluminas which have been autoclaved under steam pressure can be cited.
  • the catalyst (C 2 ) used in the second catalytic bed will preferably be incorporated on a support having a more acidic character than the support of the catalyst (C l ): its acidity, determined born as above by adsorption of ammonia, will preferably be greater than 30 joules / g. Its surface is preferably between 150 and 350 m 2 / g, and its pore volume preferably between 0.4 and 1 cm 3 / g. Mention may be made, as supports meeting these characteristics of alumina y ex boehmite or it ex bayerite, or else supports of the alumina / magnesia or silica / magnesia type containing approximately 5 to 10% by weight of magnesia.
  • a mixture of heavy asphaltic oil and hydrogen is sent by line 1 to the catalytic hydrodemetallization reactor 2, then by line 3 to the water reduction reduction reactor 4.
  • the effluent is sent by line 5 preferably in the presence a supply of hydrogen supplied by line 6 to reactor 7 containing a first bed of catalyst 8 and a second bed of catalyst 9.
  • the final product is drawn off through line 10.
  • the fillers which can be treated according to the invention are, for example, crude oils, vacuum residues, atmospheric residues, shale oil or oil sands oils or asphalts. Oils most often have a density greater than: (dl 5 ) 0.965, an API degree less than 15.1, an asphaltene content (determined with n-heptane) greater than 5% by weight, a metal content ( Ni + V) greater than 200 ppm by weight and a viscosity greater than 50 cSt (50 mm 2 / s) at 100 ° C.
  • Figures 2 to 5 show photomicrographs of catalyst A taken using a JEOL brand scanning electron microscope, model JSM 35 CF, at respective magnifications 300, 3000, 10 000 and 20 000.
  • the scales indicated on each photograph allow measure the dimensions of observable details.
  • the dark parts correspond to the porosity, while the light parts correspond to the catalytic material.
  • the catalyst A does indeed have the “sea urchin” structure according to the invention, namely a juxtaposition of agglomerates having for the most part an average dimension of 3.5 micrometers, each agglomerate being formed of elongated needle-like plates, generally assembled radially with respect to the center of the agglomerates.
  • FIG. 6 is a photomicrograph taken at nominal magnification 110,000 with a scanning transmission electron microscope (S.T.E.M. VG HB5). The dark areas this time correspond to the catalytic material. The scale of this micrograph is 9 nanometers per millimeter.
  • the intervals delimited by opposite arrows marked 1 and 2 correspond respectively to the traces of needle-like plates arranged perpendicularly and parallel to the plane of the image. The intervals 1 therefore give an approximate measurement of the thickness of the wafers and the interval 2 a measurement of the width of the wafers, that is to say approximately 2 to 4 nanometers and 60 nanometers respectively, the wafers of FIG.
  • the ratio of the average length to the average width is therefore approximately 8 to 16 and the ratio of the average length to the average thickness is approximately 120 to 480.
  • FIG. 1 shows in particular the cumulative porous distribution curve of the catalyst C.
  • This catalyst is a commercial catalyst sold by the French company PRO-CATALYSE under the name LD 145.
  • Its support is of the alumina y type, having a specific surface of 210 m 2 / g, the pore volume being 0.52 cm 3 / g; this support has a heat of neutralization by adsorption of NH 3 of 40 joules / g.
  • This catalyst is a commercial catalyst sold by the French company PRO-CATALYSE under the name HR 306.
  • the weight ratio of catalyst from the 2nd bed to the 1st bed is therefore 4.
  • the temperature in the reactor is between 370 and 400 ° C, the pressure being 140 bars.
  • the hourly flow rate of liquid charge is 0.5 m 3 / m 3 / h, the quantity of hydrogen relative to the charge is 1,200 Nm 3 / m 3 .
  • the process therefore made it possible to transform a heavy, viscous crude, non-transportable, with a high content of impurities, into a stable synthetic crude, easily transportable, with a low content of impurities.
  • the service life of the catalysts is exceptional, given the nature of the charge.
  • the test was stopped after 2300 hours, while the activity of the catalyst in step (a) still represented 50% of the initial activity.
  • the retention power of this catalyst is exceptional (130 g of fixed metals per 100 g of fresh catalyst).

Landscapes

  • 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)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP83402494A 1982-12-30 1983-12-21 Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères Expired EP0113283B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8222209 1982-12-30
FR8222209A FR2538811A1 (fr) 1982-12-30 1982-12-30 Procede de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus legeres

Publications (2)

Publication Number Publication Date
EP0113283A1 EP0113283A1 (fr) 1984-07-11
EP0113283B1 true EP0113283B1 (fr) 1987-05-13

Family

ID=9280767

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83402494A Expired EP0113283B1 (fr) 1982-12-30 1983-12-21 Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères

Country Status (7)

Country Link
US (1) US4511458A (enrdf_load_stackoverflow)
EP (1) EP0113283B1 (enrdf_load_stackoverflow)
JP (1) JPS59166589A (enrdf_load_stackoverflow)
CA (1) CA1226842A (enrdf_load_stackoverflow)
DE (1) DE3371535D1 (enrdf_load_stackoverflow)
FR (1) FR2538811A1 (enrdf_load_stackoverflow)
ZA (1) ZA839686B (enrdf_load_stackoverflow)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8372267B2 (en) 2008-07-14 2013-02-12 Saudi Arabian Oil Company Process for the sequential hydroconversion and hydrodesulfurization of whole crude oil
US8491779B2 (en) 2009-06-22 2013-07-23 Saudi Arabian Oil Company Alternative process for treatment of heavy crudes in a coking refinery
US8632673B2 (en) 2007-11-28 2014-01-21 Saudi Arabian Oil Company Process for catalytic hydrotreating of sour crude oils
US9260671B2 (en) 2008-07-14 2016-02-16 Saudi Arabian Oil Company Process for the treatment of heavy oils using light hydrocarbon components as a diluent

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4626340A (en) * 1985-09-26 1986-12-02 Intevep, S.A. Process for the conversion of heavy hydrocarbon feedstocks characterized by high molecular weight, low reactivity and high metal contents
DE3536688A1 (de) * 1985-10-15 1987-04-16 Hoechst Ag Wasserloesliche disazoverbindungen, verfahren zu deren herstellung und ihre verwendung als farbstoffe
US5024750A (en) * 1989-12-26 1991-06-18 Phillips Petroleum Company Process for converting heavy hydrocarbon oil
JP2966985B2 (ja) * 1991-10-09 1999-10-25 出光興産株式会社 重質炭化水素油の接触水素化処理方法
AU655897B2 (en) * 1992-02-21 1995-01-12 Idemitsu Kosan Co. Ltd Process for hydrotreating heavy hydrocarbon oil
RU2129139C1 (ru) * 1997-07-01 1999-04-20 Акционерное общество открытого типа "Нижегороднефтеоргсинтез" Способ получения моторных топлив
US6569318B2 (en) 2000-02-23 2003-05-27 Institut Francais Du Petrole Process for conversion of hydrocarbons on a catalyst with controlled acidity
WO2003066215A1 (fr) * 2002-02-06 2003-08-14 Japan Energy Corporation Procede de preparation de catalyseur d'hydrogenation de purification
US7095867B2 (en) * 2004-04-30 2006-08-22 Altec Lansing Technologies, Inc. Portable audio reproduction system
US8480881B2 (en) * 2009-06-11 2013-07-09 Board Of Regents, The University Of Texas System Synthesis of acidic silica to upgrade heavy feeds
CN111100678A (zh) * 2018-10-26 2020-05-05 中国石油化工股份有限公司 一种利用上流式反应器加氢处理渣油的方法
CN111100676A (zh) * 2018-10-26 2020-05-05 中国石油化工股份有限公司 一种催化剂级配方法及其在渣油加氢处理方法中的应用
CN111097547A (zh) * 2018-10-26 2020-05-05 中国石油化工股份有限公司 渣油加氢处理催化剂载体、催化剂及其制备方法

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3429801A (en) * 1965-12-06 1969-02-25 Universal Oil Prod Co Two-stage hydrorefining of asphaltene-containing oils
US3696027A (en) * 1970-01-12 1972-10-03 Chevron Res Multi-stage desulfurization
US3640817A (en) * 1970-05-13 1972-02-08 Universal Oil Prod Co Hydrocarbonaceous black oil conversion process
US3716479A (en) * 1970-12-23 1973-02-13 Mobil Oil Corp Demetalation of hydrocarbon charge stocks
US3770617A (en) * 1970-12-28 1973-11-06 Exxon Research Engineering Co Hydrodesulfurization with a specified pore size distribution in silica-stabilized alumina
US3730875A (en) * 1971-02-16 1973-05-01 Universal Oil Prod Co Combination process for black oil conversion
US3947347A (en) * 1972-10-04 1976-03-30 Chevron Research Company Process for removing metalliferous contaminants from hydrocarbons
FR2268860B1 (enrdf_load_stackoverflow) * 1974-04-24 1977-06-24 Inst Francais Du Petrole
FR2277140A1 (fr) * 1974-07-04 1976-01-30 Leuna Werke Veb Procede de fabrication de fuels ainsi que de distillats moyens et d'essences pauvres en soufre a partir de residus de la distillation du petrole
US4212729A (en) * 1978-07-26 1980-07-15 Standard Oil Company (Indiana) Process for demetallation and desulfurization of heavy hydrocarbons
US4225421A (en) * 1979-03-13 1980-09-30 Standard Oil Company (Indiana) Process for hydrotreating heavy hydrocarbons
DE3020518C2 (de) * 1980-05-30 1987-01-08 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur Aufarbeitung von schweren, asphaltenhaltigen Kohlenwasserstoff-Ölen
FR2486094B1 (enrdf_load_stackoverflow) * 1980-07-02 1985-03-22 Catalyse Soc Prod Francais
FR2496631B1 (fr) * 1980-12-23 1989-06-30 Rhone Poulenc Ind Procede de preparation d'agglomeres d'alumine
JPS57123290A (en) * 1981-01-25 1982-07-31 Chiyoda Chem Eng & Constr Co Ltd Method for converting heavy hydrocarbon oil into light fractions
US4421633A (en) * 1981-03-13 1983-12-20 Mobil Oil Corporation Low pressure cyclic hydrocracking process using multi-catalyst bed reactor for heavy liquids
FR2508898B1 (fr) * 1981-07-03 1986-11-14 Inst Francais Du Petrole Procede de conversion de coupes riches en hydrocarbures polyaromatiques en methane, ethane et eventuellement benzene
CA1195278A (en) * 1981-09-28 1985-10-15 Chevron Research And Technology Company Layered residua treatment catalyst process and temperature profile
FR2516932B1 (fr) * 1981-11-24 1985-07-19 Inst Francais Du Petrole Procede de conversion d'huiles lourdes ou de residus petroliers en hydrocarbures gazeux et distillables
FR2528721B1 (fr) * 1982-06-17 1986-02-28 Pro Catalyse Ste Fse Prod Cata Catalyseur supporte presentant une resistance accrue aux poisons et son utilisation en particulier pour l'hydrotraitement de fractions petrolieres contenant des metaux

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8632673B2 (en) 2007-11-28 2014-01-21 Saudi Arabian Oil Company Process for catalytic hydrotreating of sour crude oils
US8372267B2 (en) 2008-07-14 2013-02-12 Saudi Arabian Oil Company Process for the sequential hydroconversion and hydrodesulfurization of whole crude oil
US9260671B2 (en) 2008-07-14 2016-02-16 Saudi Arabian Oil Company Process for the treatment of heavy oils using light hydrocarbon components as a diluent
US8491779B2 (en) 2009-06-22 2013-07-23 Saudi Arabian Oil Company Alternative process for treatment of heavy crudes in a coking refinery

Also Published As

Publication number Publication date
FR2538811A1 (fr) 1984-07-06
CA1226842A (fr) 1987-09-15
US4511458A (en) 1985-04-16
EP0113283A1 (fr) 1984-07-11
JPS59166589A (ja) 1984-09-19
FR2538811B1 (enrdf_load_stackoverflow) 1985-03-15
ZA839686B (en) 1985-08-28
DE3371535D1 (en) 1987-06-19

Similar Documents

Publication Publication Date Title
EP0113284B1 (fr) Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères
EP0113283B1 (fr) Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères
EP0098764B1 (fr) Catalyseur supporté présentant une résistance accrue aux poisons et son utilisation en particulier pour l'hydrotraitement de fractions pétrolières contenant des métaux
EP1577007B1 (en) Hydrotreating catalyst for gas oil, process for producing the same, and method of hydrotreating gas oil
EP1579909B1 (fr) Procédé d'hydrotraitement et d'hydroconversion de fractions pétrolières contenant des métaux en présence d'un catalyseur supporté de forme shpérique dopé avec du phosphore.
EP0113297B1 (fr) Procédé d'hydrotraitement convertissant en au moins deux étapes une fraction lourde d'hydrocarbures contenant des impuretés soufrées et des impuretés métalliques
CA2615210C (fr) Procede d'hydroconversion en slurry de charges hydrocarbonees lourdes en presence d'une phase active dispersee et d'un oxyde a base d'alumine
CA2615225C (fr) Procede d'hydroconversion en phase slurry de charges hydrocarbonees lourdes et ou de charbon utilisant un catalyseur supporte
CA2291523A1 (fr) Catalyseur d'hydrotraitement de charges hydrocarbonees dans un reacteur a lit fixe
FR2764214A1 (fr) Procede et masses de captation pour l'elimination du mercure et de l'arsenic dans les coupes hydrocarbonees
FR2787040A1 (fr) Hydrotraitement de charges hydrocarbonees dans un reacteur en lit bouillonnant
EP0884372B1 (fr) Hydrotraitement de charges hydrocarbonées dans un réacteur en lit bouillonnant
KR20140095507A (ko) 자기-활성화 수소첨가처리 촉매 및 중질 탄화수소 공급원료의 처리 방법
EP0991466B1 (fr) Extrudes d'alumine, leurs procedes de preparation et leur utilisation comme catalyseurs ou supports de catalyseurs
FR2534828A1 (fr) Catalyseurs a base d'alumine, de silice ou de silice-alumine, leur preparation et leur utilisation dans le domaine de l'hydrotraitement des huiles d'hydrocarbures
EP4251713A1 (fr) Procede d'hydrogenation selective d'une essence en presence d'un catalyseur sur support meso-macroporeux
FR2556363A1 (fr) Procede d'hydrotraitement d'hydrocarbures
JPH0295443A (ja) 残油の水素化処理触媒
CA1207302A (fr) Catalyseurs a base d'alumine, de silice ou de silice- alumine, leur preparation et leur utilisation pour l'hydrotraitement des huiles d'hydrocarbures
EP4251716A1 (fr) Procede de captation d'impuretes organometalliques en presence d'une masse de captation sur support meso-macroporeux
BE893161A (fr) Catalyseur se pretant a l'hydrodemetallation d'alimentations lourdes et procede d'hydrodemetallation d'alimentations lourdes
FR3156132A1 (fr) Procede de preparation d’une alumine comprenant du lanthane pour l’hydrotraitement de distillats sous vide

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): BE DE GB IT NL SE

17P Request for examination filed

Effective date: 19841122

ITF It: translation for a ep patent filed
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE GB IT NL SE

REF Corresponds to:

Ref document number: 3371535

Country of ref document: DE

Date of ref document: 19870619

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
ITTA It: last paid annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19910924

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19911121

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19911129

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19911231

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19920207

Year of fee payment: 9

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19921221

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19921222

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19921231

BERE Be: lapsed

Owner name: INSTITUT FRANCAIS DU PETROLE

Effective date: 19921231

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19930701

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19921221

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19930901

EUG Se: european patent has lapsed

Ref document number: 83402494.5

Effective date: 19930709