EP0099141B1 - Procédé pour la production de mélanges d'hydrocarbures à faible teneur en asphaltène - Google Patents

Procédé pour la production de mélanges d'hydrocarbures à faible teneur en asphaltène Download PDF

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Publication number
EP0099141B1
EP0099141B1 EP83200869A EP83200869A EP0099141B1 EP 0099141 B1 EP0099141 B1 EP 0099141B1 EP 83200869 A EP83200869 A EP 83200869A EP 83200869 A EP83200869 A EP 83200869A EP 0099141 B1 EP0099141 B1 EP 0099141B1
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Prior art keywords
deasphalted oil
feed
asphaltic bitumen
asphaltenes
product
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German (de)
English (en)
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EP0099141A1 (fr
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Petrus M.M. Blauwhoff
Jacobus M.H. Dirkx
Jacobus C/O Shell Canada Ltd. Eilers
Karl Heinz Röbschläger
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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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
    • C10G67/0463—The hydrotreatment being a hydrorefining
    • 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 a process for the production of deasphalted oils and hydrocarbon oil distillates from asphaltenes-containing hydrocarbon mixtures.
  • solvent deasphalting may be used to separate from an atmospheric residue a deasphalted oil which may be subjected to catalytic cracking in the presence or in the absence of hydrogen.
  • DA solvent deasphalting
  • Another option is to separate an atmospheric residue by vacuum distillation into a vacuum distillate and a vacuum residue, to separate a deasphalted oil from the vacuum residue using DA and to subject both the vacuum distillate and the deasphalted oil to catalytic cracking in the presence or in the absence of hydrogen.
  • a drawback to the conventional DA treatment, in which an asphaltenes-containing feed is separated in one step into a deasphalted oil as the desired main product and an asphaltic bitumen as a by-product, is that if a sufficiently high yield of deasphalted oil is to be realised, one must generally accept a deasphalted oil of unsatisfactory quality.
  • the quality of the deasphalted oil should be taken to be its suitability to be converted into hydrocarbon oil distillates by catalytic cracking in the presence or in the absence of hydrogen. This suitability becomes better according as the deasphalted oil has, among other things, lower asphaltenes, metal and sulphur contents.
  • Deasphalted oil 1 a high-quality deasphalted oil
  • deasphalted oil 2 a deasphalted oil of lower quality
  • asphaltic bitumen an asphaltic bitumen.
  • Deasphalted oil 1 differs from deasphalted oil 2 mainly by its considerably lower asphaltenes, metal and sulphur contents.
  • One of the pretreatments investigated was a catalytic hydrotreatment (for the sake of brevity hereinafter referred to as "HT") in which the asphaltenes-containing feed is converted into a product having a reduced asphaltenes content, from which one or more distillate fractions are separated whilst the residue is used as the feed for the two-step DA treatment.
  • HT catalytic hydrotreatment
  • the yield and quality of the deasphalted oils and the asphaltic bitumen that play a role the yield of light product is of great importance as well.
  • the quality of the asphaltic bitumen should be taken to be its suitability to serve as fuel oil component. This suitability is better according to the asphatic bitumen has lower metal and sulphur contents and lower viscosity and density.
  • procedure b) is much to be preferred to procedure a).
  • the present patent application therefore relates to a process for the production of deasphalted oils and hydrocarbon oil distillates from asphaltenes-containing hydrocarbon mixtures, in which a HT is used to convert an asphaltenes-containing hydrocarbon mixture into a product with a reduced asphaltenes content which is separated by distillation into one or more distillate fractions and a residual fraction and in which two-step DA is used to separate the residual fraction into a deasphalted oil 1 of high quality, a deasphalted oil 2 of lower quality and an asphaltic bitumen.
  • the feed used is an asphaltenes-containing hydrocarbon mixture.
  • a suitable parameter for the assessment of the asphaltenes content of a hydrocarbon mixture and for the reduction of the asphaltenes content which occurs when a HT is applied to an asphaltenes-containing hydrocarbon mixture is the Ramsbottom Carbon Test value (RCT).
  • RCT Ramsbottom Carbon Test value
  • the process is preferably applied to hydrocarbon mixtures which substantially boil above 350°C and more than 35%w of which boils above 520°C and which have an RCT of more than 7.5%w. Examples of such hydrocarbon mixtures are residues obtained in the distillation of crude mineral oils and heavy hydrocarbon mixtures obtained from shale and tar sand.
  • the process may also be applied to heavy crude mineral oils, to residues obtained in the distillation of products developed in the thermal cracking of hydrocarbon mixtures and to asphaltic bitumen obtained in the solvent deasphalting of asphaltenes-containing hydrocarbon mixtures.
  • the process according to the invention is very suitable for application to residues obtained in the vacuum distillation of atmospheric distillation residues of crude mineral oils.
  • the process according to the invention is also very suitable for application to residues obtained in the vacuum distillation of atmospheric distillation residues of products developed in the thermal cracking of asphaltenes-containing hydrocarbon mixtures.
  • the feed available for the process according to the invention is an atmospheric distillation residue
  • the separated vacuum distillate can be subjected to thermal cracking or to catalytic cracking in the presence or in the absence of hydrogen to convert it into light hydrocarbon oil distillates.
  • Asphaltenes-containing hydrocarbon mixtures generally contain a considerable proportion of metals, in particular vanadium and nickel. If such hydrocarbon mixtures are subjected to a catalytic treatment, for instance a HT for the reduction of the asphaltenes content, as in the process according to the invention, these metals will deposit on the catalyst used in the HT and thus shorten its life.
  • asphaltenes-containing hydrocarbon mixtures with a vanadium+nickel content of more than 50 parts per million by weight (ppmw) should preferably be subjected to demetallization before being contacted with the catalyst used in the HT.
  • This demetallization may very suitably be carried out by contacting the asphaltenes-containing hydrocarbon mixture in the presence of hydrogen with a catalyst consisting more than 80%w of silica.
  • a catalyst consisting more than 80%w of silica Both catalysts consisting entirely of silica and catalysts containing one or more metals having hydrogenating activity, in particular a combination of nickel and vanadium, present on a carrier support substantially consisting of silica, are suitable for the purpose. If in the process according to the invention a catalytic demetallization in the presence of hydrogen is applied to an asphaltenes-containing feed, this demetallization may be carried out in a separate reactor.
  • the two processes may also very suitably be carried out in the same reactor, which will contain a bed of the demetallization catalyst and a bed of the catalyst used in the HT, successively.
  • Suitable catalysts for carrying out the HT are those containing at least one metal chosen from the group formed by nickel and cobalt and in addition at least one metal chosen from the group formed by molybdenum and tungsten supported on a carrier, which carrier consists more than 40%w of alumina.
  • Very suitable catalysts for use in the HT are those comprising the metal combinations nickel/molybdenum or cobalt/molybdenum on alumina as a carrier.
  • the HT is preferably carried out at a temperature of from 300-500°C and in particular of from 350-450°C, a pressure of from 50-300 bar and in particular of from 75-200 bar, a space velocity of from 0.02-10 g.g-'.h-' and in particular of from 0.1-2 g.g -1 .h -1 and a H 2 /feed ratio of from 100-5000 Ni.kg- 1 and in particular of from 500-2000 Ni.kg- 1 .
  • the conditions used in a possible catalytic demetallization in the presence of hydrogen the same preference applies as that stated hereinbefore for the HT for the reduction of the asphaltenes content.
  • the HT is preferably carried out in such a manner that it yields a product the Cs fraction of which meets the following requirements:
  • a product with a reduced asphaltenes content is obtained from which one or more distillate fractions and a heavy fraction are separated.
  • the distillate fractions separated from the product may be atmospheric distillates only, but it is preferred to separate a vacuum distillate from the product as well. This vacuum distillate may be converted into light hydrocarbon oil distillates in the manners indicated hereinbefore.
  • two-step DA treatment is applied to a distillation residue obtained as one of the products of the HT.
  • Suitable solvents for carrying out the DA treatment are waxy hydrocarbons having 3-7 carbon atoms per molecule, such as propane, n-butane isobutane, n-pentane, isopentane and mixtures thereof, such as mixtures of propane and n-butane and mixtures of n-butane and isobutane.
  • Suitable solvent/oil weight ratios lie between 7:1 and 1:1.
  • the DA treatment is preferably carried out at elevated temperature and pressure.
  • the two-step DA treatment may essentially be carried out in two ways.
  • the residue from the HT to be treated is subjected to extraction under mild conditions in which the residue is separated into a deasphalted oil 1 and a "light" asphaltic bitumen and subsequently the light asphaltic bitumen is subjected in the second step to a second extraction in which it is separated into a deasphalted oil 2 and the final asphaltic bitumen as a by-product.
  • the same solvent can be used in both steps and the degree of extraction is controlled with the aid of the temperature (temperature in the first step higher than in the second step).
  • Different solvents may also be used, for instance propane in the first step and n-butane in the second step.
  • the residue from the HT to be treated is subjected to extraction under severe conditions in which the residue is separated into a deasphalted oil and the final asphaltic bitumen as a by-product and subsequently the deasphalted oil is separated in the second step into a deasphalted oil 1 and a deasphalted oil 2.
  • the mixture of deasphal t ed oil and solvent coming from the extractor need only be fed into a settler in which a higher temperature prevails than that used in the first step.
  • each one of these embodiments may be assigned to one of two main classes, depending on whether the asphaltenes-containing feed is subjected to the HT immediately (class I) or whether the asphaltenes-containing feed is first subjected to thermal cracking (for the sake of brevity hereinafter referred to as TC) and the HT is applied to a residual fraction of the thermally cracked product (class II).
  • the embodiments belonging to class I may further be arranged according to whether the apparatus in which the process is carried out is confined to a HT zone and a two-step DA zone (class IA) or whether the apparatus in addition to a HT zone and a two-step DA zone also includes a TC zone (class IB), a CC zone (IC) or both a TC zone and a CC zone (class ID), in which the deasphalted oil 2 and/or the asphaltic bitumen separated in the two-step DA zone, are further processed.
  • CC as used hereinbefore should be taken to refer to a special type of catalytic, cracking for the preparation of light hydrocarbon oil distillates, in which the feed used is a de- asphalfed oil 2.
  • This feed is distinguished from the feed which is normally used in a catalytic cracking process by the fact that the deasphalted oil 2 has, among other things, a much higher RCT and a much higher metal content.
  • the object is to obtain as complete as possible a conversion of the asphaltenes-containing feed into deasphalted oil and hydrocarbon oil distillates
  • Carrying out the process according to the invention by using a TC treatment and/or a CC treatment yields cracked products from which one or more distillate fractions are separated.
  • These distillate fractions may be atmospheric distillates only, but preferably a vacuum distillate should also be separated from the cracked products. This vacuum distillate may be converted into light hydrocarbon oil distillates by the methods mentioned hereinbefore.
  • the process according to the invention is carried out in an apparatus which includes a TC zone, whilst the streams which are fed into this TC zone consist of one or more relatively low-asphaltenes streams-such as a deasphalted oil 2-as well as of one or more relatively asphaltenes-rich streams-such as asphaltic bitumen separated in the process and/or the asphaltenes-containing feed which is to be processed with the aid of the process-, it is preferred to use a TC zone which includes two cracking units and to crack the types of feed separately into products from which one or more distillate fractions and a residual fraction are separated.
  • a TC zone which includes two cracking units and to crack the types of feed separately into products from which one or more distillate fractions and a residual fraction are separated.
  • a heavy fraction of the cracked product coming from the cracking unit in which a relatively low-asphaltenes feed is processed is preferably recirculated to that cracking unit.
  • a TC zone which includes two cracking units, then, from the product obtained in the cracking unit in which the relatively asphaltenes-rich feed is cracked, a relatively low-asphaltenes heavy fraction may be separated, if desired, and the latter may be used as a feed component for the cracking unit in which the relatively low-asphaltenes feed is processed.
  • a TC zone which includes two cracking units
  • the process is carried out in an apparatus consisting of a HT zone composed of a catalytic hydrotreatment unit ⁇ (11), an atmospheric distillation unit (15) and a vacuum distillation unit (16) and a two-step DA zone (12), successively.
  • An asphaltenes-containing hydrocarbon mixture (1), together with hydrogen (20), is subjected to a catalytic hydrotreatment.
  • the hydrotreated product (21) is separated by atmospheric distillation into a gas fraction (22), an atmospheric distillate (2A) and an atmospheric residue (23).
  • the atmospheric residue (23) is separated by vacuum distillation into a vacuum distillate (2B) and a vacuum residue (3).
  • the vacuum residue (3) is separated by two-step deasphalting into a deasphalted oil 1 (stream 4), a deasphalted oil 2 (stream 5) and an asphaltic bitumen (6).
  • the process is carried out in an apparatus consisting of a HT zone composed of a catalytic hydrotreatment unit (11), an atmospheric distillation unit (15) and a vacuum distillation unit (16), a two-step DA zone (12) and a TC zone composed of a thermal cracking unit (13), a second atmospheric distillation unit (17) and a second vacuum distillation unit (18), successively.
  • a HT zone composed of a catalytic hydrotreatment unit (11), an atmospheric distillation unit (15) and a vacuum distillation unit (16), a two-step DA zone (12) and a TC zone composed of a thermal cracking unit (13), a second atmospheric distillation unit (17) and a second vacuum distillation unit (18), successively.
  • An asphaltenes-containing hydrocarbon mixture (1) is mixed with a recirculation stream (8) and the mixture (29), together with hydrogen (20), is subjected to a catalyst hydrotreatment.
  • the hydrotreated product (21) is separated by atmospheric distillation into a gas fraction (22), an atmospheric distillate (2A) and an atmospheric residue (23).
  • the atmospheric residue (23) is separated by vacuum distillation into a vacuum distillate (2B) and a vacuum residue (3).
  • the vacuum residue (3) is separated by two-step solvent deasphalting into a deasphalted oil 1 (stream 4), a deasphalted oil 2 (stream 5) and an asphaltic bitumen (6).
  • the asphaltic bitumen (6) is divided into two portions (30) and (31). Portion (30) is subjected to thermal cracking.
  • the thermally cracked product (24) is separated by atmospheric distillation into a gas fraction (25), an atmospheric distillate (7A) and an atmospheric residue (26).
  • the atmospheric residue (26) is separated by vacuum distillation into a vacuum distillate
  • the process is carried out in an apparatus consisting of a HT zone composed of a catalytic hydrotreatment unit (11), an atmospheric distillation unit (15) and a vacuum distillation unit (16), a two-step DA zone (12) and a CC zone composed of a catalytic cracking unit (14) and a second atmospheric distillation unit (19), successively.
  • An asphaltenes-containing hydrocarbon mixture (1) is mixed with a recirculation stream (10) and the mixture (32), together with hydrogen (20), is subjected to a catalytic hydrotreatment.
  • the hydrotreated product (21) is separated by atmospheric distillation into a gas fraction (22), an atmospheric distillate (2A) and an atmospheric residue (23).
  • the atmospheric residue (23) is separated by vacuum distillation into a vacuum distillate (2B) and a vacuum residue (3).
  • the vacuum residue (3) is separated by two-step solvent deasphalting into a deasphalted oil 1 (stream 4), a deasphalted oil 2 (stream 5) and an asphaltic bitumen (6).
  • the deasphalted oil 2 (stream 5) is subjected to catalytic cracking.
  • the catalytically cracked product (27) is separated by atmospheric distillation into a gas fraction (28), an atmospheric distillate (9) and an atmospheric residue (10).
  • the process is carried out in an apparatus consisting of a HT zone composed of a catalytic hydrotreatment unit (11), an atmospheric distillation unit (15) and a vacuum distillation unit (16), a two-step DA zone (12), a TC zone composed of a thermal cracking unit (13), a second atmospheric distillation unit (17) and a second vacuum distillation unit (18) and a CC zone composed of a catalytic cracking unit (14) and a third atmospheric distillation unit (19), successively.
  • An asphaltenes-containing hydrocarbon mixture (1) is mixed with a recirculation stream (34) and the mixture (33), together with hydrogen (20), is subjected to a catalytic hydrotreatment.
  • the hydrotreated product (21) is separated by atmospheric distillation into a gas fraction (22), an atmospheric distillate (2A) and an atmospheric residue (23).
  • the atmospheric residue (23) is separated by vacuum distillation into a vacuum distillate (2B) and a vacuum residue (3).
  • the vacuum residue (3) is separated by two-step solvent deasphalting into a deasphalted oil 1 (stream 4), a deasphalted oil 2 (stream 5) and an asphaltic bitumen (6).
  • the asphaltic bitumen (6) is divided into two portions (30) and (31). Portion (30) is subjected to thermal cracking.
  • the thermally cracked product (24) is separated by atmospheric distillation into a gas fraction (25), an atmospheric distillate (7A) and an atmospheric residue (26).
  • the atmospheric residue (26) is separated by vacuum distillation into a vacuum distillate (7B) and a vacuum residue (8).
  • the deasphalted oil 2 (stream 5) is subjected to catalytic cracking.
  • the catalytically cracked product (27) is separated by atmospheric distillation into a gas fraction (28), an atmospheric distillate (9) and an atmospheric residue (10).
  • Streams (8) and (10) are mixed to form the recirculation stream (34).
  • the process is carried out in an apparatus consisting of a TC zone composed of a thermal cracking unit (13), an atmospheric distillation unit (17) and a vacuum distillation unit (18), a HT zone composed of a catalytic hydrotreatment unit (11), a second atmospheric distillation unit (15) and a second vacuum distillation unit (16) and a two-step DA zone (12), successively.
  • An asphaltenes-containing hydrocarbon mixture (1) is subjected to thermal cracking.
  • the thermally cracked product (24) is separated by atmospheric distillation into a gas fraction (25), an atmospheric distillate (7A) and an atmospheric residue (26).
  • the atmospheric residue (26) is separated by vacuum distillation into a vacuum distillate (7B) and a vacuum residue (8).
  • the vacuum residue (8), together with hydrogen (20), is subjected to a catalytic hydrotreatment.
  • the hydrotreated product (21) is separated by atmospheric distillation into a gas fraction (22), an atmospheric distillate (2A) and an atmospheric residue (23).
  • the atmospheric residue (23) is separated by vacuum distillation into a vacuum distillate (2B) and a vacuum residue (3).
  • the vacuum residue (3) is separated by two-step solvent deasphalting into a deasphalted oil 1 (stream 4), a deasphalted oil 2 (stream 5) and an asphaltic bitumen (6).
  • the present patent application also includes apparatuses for carrying out the embodiments according to the process according to the invention which substantially correspond with those schematically represented in Figures I-VII.
  • the starting material was an asphaltenes-containing hydrocarbon mixture obtained as a residue in the vacuum distillation of an atmospheric distillation residue of a crude mineral oil.
  • the vacuum residue boiled substantially above 520°C and had an RCT of 18.8%w, an overall vanadium and nickel content of 167 ppmw and a sulphur content of 5.4%w.
  • the process was carried out according to the flow diagrams A-E. The following conditions were used in the various zones.
  • the catalytic hydrotreatment unit consisted of two reactors, the first of which was filled with a NiN/Si0 2 catalyst containing 0.5 parts by weight (pbw) of nickel and 2.0 pbw of vanadium per 100 pbw of silica and the second of which was filled with a Ni/Mo/AI 2 0 3 catalyst containing 4 pbw of nickel and 12 pbw of molybdenum per 100 pbw of alumina.
  • the catalysts were used in a volume ratio 1:4.
  • the HT was carried out at a hydrogen pressure at 150 bar, a space velocity (measured over the two reactors) of 0.5 kg of feed per litre of catalyst per hour, a H 2 /feed ratio of 1000 NI per kg and an average temperature of 410°C in the first reactor and 390°C in the second reactor.
  • the two-step DA treatment was carried out by contacting the feed to be deasphalted in the first step (in an extractor) with a n-butane/isobutane mixture (weight ratio 65:35) at a temperature of 110°C, a pressure of 40 bar and a solvent/oil weight ratio of 2:1 and, after the asphaltic bitumen has been separated off, separating the deasphalted oil in a second step (in a settler) at a temperature of 140°C and a pressure of 40 bar into a deasphalted oil 1 and a deasphalted oil 2.
  • the CC treatment was carried out at a temperature of 510°C, a pressure of 2.2 bar, a space velocity of 2 kg.kg-'.h- 1 and a catalyst renewal rate of 1.0 pbw of catalyst per 1000 pbw of oil and using a zeolite cracking catalyst.
  • Example 6 the two-step DA treatment was carried out in substantially the same way as described in the Examples 1-5, with the distinction that the temperature prevailing in the settler described in Example 6 was 144°C.
  • asphaltenes-containing hydrocarbon mixture (1) used as starting material was 100 pbw of vacuum residue.
  • Table II lists the yields of final products obtained in the experiments described in Examples 1-7.
  • Table III lists the properties of the final products obtained in the experiments described in Examples 1-7.
  • Example 4 describing experiments in which both a TC treatment and a CC treatment are used, provides a combination of the advantages mentioned for Examples 2 and 3.
  • Comparison of Examples 1 and 5 shows that application of a TC treatment to the feed for the HT produces considerably higher yields of hydrocarbon oil distillates.

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Claims (16)

1. Procédé pour la production d'huiles désal- phaltées et de distillats d'huiles hydrocarbures à partir de mélanges d'hydrocarbures contenant des asphaltènes, caractérisé en ce que l'on utilise un hydrotraitement catalytique pour transformer le mélange d'hydrocarbures contenant des asphaltènes en un produit ayant une teneur en asphaltènes réduite que l'on sépare par distillation en une ou plusieurs fractions de distillats et une fraction résiduelle et en ce que l'on utilise une désalphaltation par solvant en deux étapes pour séparer la fraction résiduelle en une huile désalphaltée 1 de qualité supérieure, une huile désalphaltée 2 de qualité inférieure et un bitume asphaltique.
2. Procédé selon la revendication 1, caractérisé en ce que la charge utilisée est un mélange d'hydrocarbures qui bout sensiblement au-dessus de 350°C et dont plus de 35% en poids bout au-dessus de 520°C et qui a une RCT (valeur de Ramsbottom) supérieure à 7,5% en poids, de préférence un résidu obtenu lors de la distillàtion sous vide d'un résidu de distillation atmosphérique d'une huile minérale brute.
3. Procédé selon la revendication 1 ou 2, caractérisé en ce que, dans l'hydrotraitement catalytique destiné à réduire la teneur en asphaltènes, on utilise un catalyseur qui comprend au moins un métal choisi dans le groupe formé par le nickel et le cobalt et, en outre, au moins un métal choisi dans le groupe formée par le molybdène et le tungstène sur un support dont plus de 40% en poids est constitué d'alumine, de préférence une combinaison métallique nickel/molybdène ou cobalt/molybdène sur support d'alumine.
4. Procédé selon la revendication 3, caractérisé en ce que, lorsqu'on utilise une charge pour l'hydrotraitement catalytique qui a une teneur en vanadium+nickel supérieure à 50 ppmp (ppm en poids), cette charge est mise en contact avec deux catalyseurs successifs dont le premier est un catalyseur de démétallisation constitué par plus de 80% en poids de silice et dont le second est un catalyseur de transformation des asphaltènes selon la revendication 3.
5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que l'hydrotraitement catalytique est réalisé à une température de 350 à 450°C, sous une pression de 75 à 200 bars, avec une vitesse spatiale de 0,1 à 2 g.g-1.h-1 et selon un rapport H2/charge de 500 à 2000 NI.kg-1.
6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'hydrotraitement catalytique est réalisé de manière que l'on obtienne un produit dont la fraction en Cs satisfasse aux exigences suivantes:
a) la RCT de la fraction en Cs est de 20 à 70% de la RCT de la charge et
b) la différence entre les pourcentages en poids des hydrocarbures bouillant au-dessous de 350°C présents dans la fraction en Cs et dans la charge est au plus de 40.
7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que la désalphaltation par solvant en deux étapes est réalisée en soumettant la fraction résiduelle séparée du produit de l'hydrotraitement catalytique dans la première étape à une extraction dans des conditions ménagées où elle est séparée en une huile désalphaltée 1 et un bitume asphaltique "léger" et en soumettant le bitume asphaltique léger dans la seconde étape à un second traitement d'extraction où il est séparé en une huile désalphaltée 2 et le bitume asphaltique final comme sous-produit du procédé.
8. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que la désalphaltation par solvant er deux étapes est réalisée en soumettant la fraction résiduelle séparée du produit de l'hydrotraitement catalytique dans la première étape à une extraction dans des conditions sévères où elle est séparée en une huile désalphaltée et le bitume asphaltique final comme sous-produit du procédé et en séparant l'huile désalphaltée dans la seconde étape en une huile désalphaltée 1 et une huile désalphaltée 2.
9. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que l'huile désalphaltée 2 ou le bitume asphaltique est utilisé comme constituant de la charge de l'hydrotraitement catalytique.
10. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que l'huile désalphaltée 2 et/ou le bitume asphaltique est soumis à un craquage thermique et en ce que un résidu de distillation du produit craqué thermiquement, de préférence à la fois un résidu de distillation du produit craqué thermiquement et le bitume asphaltique, est (sont) utilisé(s) comme constituant de la charge de l'hydrotraitement catalytique.
11. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que l'huile désalphaltée 2 est soumise à un craquage catalytique et en ce qu'un résidu de distillation du produit craqué catalytiquement, qu'il soit ou non mélangé au bitume asphaltique, est utilisé comme constituant de la charge de l'hydroitraite- ment catalytique.
12. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que l'huile désalphaltée 2 est soumise à un craquage catalytique, en ce que le bitume asphaltique est soumis à un craquage thermique et en ce que à la fois un résidu de distillation du produit craqué catalytiquement et un résidu de distillation du produit craqué thermiquement sont utilisés comme constituants de la charge de l'hydrotraitement catalytique.
13. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que le mélange d'hydrocarbures contenant des asphaltènes qui sert de charge pour le procédé est d'abord soumis à un craquage thermique et en ce qu'un résidu de distillation du produit craqué thermiquement est utilisé comme charge de l'hydrotraitement catalytique.
14. Procédé selon la revendication 13, caractérisé en ce qu'on utilise l'huile désalphaltée 2 ou le bitume asphaltique comme constituant de la charge du craquage thermique ou de l'hydrotraitement catalytique.
15. Procédé selon la revendication 13, caractérisé en ce qu'on utilise à la fois l'huile désalphaltée 2 et le bitume asphaltique comme constituants de la charge du craquage thermique.
16. Procédé selon la revendication 13, caractérisé en ce qu'on utilise l'huile désalphaltée 2 comme constituant de la charge destinée soit au craquage thermique ou à l'hydroitraitement catalytique, tandis qu'on utilise le bitume asphaltique comme constituant de la charge destinée soit à l'hydrotraitement catalytique ou au craquage thermique, respectivement.
EP83200869A 1982-07-13 1983-06-14 Procédé pour la production de mélanges d'hydrocarbures à faible teneur en asphaltène Expired EP0099141B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL8202827A NL8202827A (nl) 1982-07-13 1982-07-13 Werkwijze voor de bereiding van asfaltenenarme koolwaterstofmengsels.
NL8202827 1982-07-13

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EP0099141A1 EP0099141A1 (fr) 1984-01-25
EP0099141B1 true EP0099141B1 (fr) 1986-04-23

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EP (1) EP0099141B1 (fr)
JP (1) JPS5924790A (fr)
AU (1) AU562320B2 (fr)
CA (1) CA1198387A (fr)
DE (1) DE3363155D1 (fr)
ES (1) ES8500315A1 (fr)
MX (1) MX162539A (fr)
NL (1) NL8202827A (fr)
ZA (1) ZA835028B (fr)

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CA1222471A (fr) * 1985-06-28 1987-06-02 H. John Woods Methode pour ameliorer le rendement des produits distillables dans le craquage a diluant donneur d'hydrogene
US5013427A (en) * 1989-07-18 1991-05-07 Amoco Corportion Resid hydrotreating with resins
US10947464B2 (en) 2015-12-28 2021-03-16 Exxonmobil Research And Engineering Company Integrated resid deasphalting and gasification
US10550335B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Fluxed deasphalter rock fuel oil blend component oils
US10590360B2 (en) 2015-12-28 2020-03-17 Exxonmobil Research And Engineering Company Bright stock production from deasphalted oil
US10233394B2 (en) * 2016-04-26 2019-03-19 Saudi Arabian Oil Company Integrated multi-stage solvent deasphalting and delayed coking process to produce high quality coke
US10125318B2 (en) 2016-04-26 2018-11-13 Saudi Arabian Oil Company Process for producing high quality coke in delayed coker utilizing mixed solvent deasphalting
US10494579B2 (en) 2016-04-26 2019-12-03 Exxonmobil Research And Engineering Company Naphthene-containing distillate stream compositions and uses thereof

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL7510465A (nl) * 1975-09-05 1977-03-08 Shell Int Research Werkwijze voor het omzetten van koolwaterstoffen.
NL7602240A (nl) * 1976-03-04 1977-09-06 Shell Int Research Werkwijze voor het omzetten van koolwaterstoffen.
NL7612960A (nl) * 1976-11-22 1978-05-24 Shell Int Research Werkwijze voor het omzetten van koolwater- stoffen.
NL7702161A (nl) * 1977-03-01 1978-09-05 Shell Int Research Werkwijze voor het omzetten van koolwater- stoffen.
JPS541306A (en) * 1977-06-07 1979-01-08 Chiyoda Chem Eng & Constr Co Ltd Hydrogenation of heavy hydrocarbon oil
GB2031011B (en) * 1978-10-05 1983-01-06 Chiyoda Chem Eng Construct Co Processing heavy hydrocarbon oils
EP0068543B1 (fr) * 1981-06-25 1988-09-21 Shell Internationale Researchmaatschappij B.V. Procédé pour la préparation d'un mélange d'hydrocarbures

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ES524008A0 (es) 1984-10-01
ES8500315A1 (es) 1984-10-01
NL8202827A (nl) 1984-02-01
ZA835028B (en) 1984-03-28
MX162539A (es) 1991-05-20
DE3363155D1 (en) 1986-05-28
AU562320B2 (en) 1987-06-04
AU1672683A (en) 1984-01-19
JPS5924790A (ja) 1984-02-08
CA1198387A (fr) 1985-12-24
EP0099141A1 (fr) 1984-01-25

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