EP0246956A1 - Verfahren zur Entfernung von Asphalt aus einer Kohlenwasserstoffbeschickung - Google Patents

Verfahren zur Entfernung von Asphalt aus einer Kohlenwasserstoffbeschickung Download PDF

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Publication number
EP0246956A1
EP0246956A1 EP87401091A EP87401091A EP0246956A1 EP 0246956 A1 EP0246956 A1 EP 0246956A1 EP 87401091 A EP87401091 A EP 87401091A EP 87401091 A EP87401091 A EP 87401091A EP 0246956 A1 EP0246956 A1 EP 0246956A1
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Prior art keywords
solvent
carbon atoms
hydrocarbon
fraction
volume
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EP87401091A
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English (en)
French (fr)
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EP0246956B1 (de
Inventor
Didier Chombart
François-Xavier Cormerais
Michel Laborde
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TotalEnergies Marketing Services SA
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Total France SA
Compagnie de Raffinage et de Distribution Total France SA
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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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
    • C10G53/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics

Definitions

  • the present invention relates to a process for deasphalting a heavy hydrocarbon feed.
  • heavy hydrocarbon charge is meant, within the meaning of the present invention, a charge having a density at 15 ° C greater than about 930 kg / m3, composed essentially of hydrocarbons, but also containing other chemical compounds which, in addition to carbon and hydrogen atoms have heteroatoms, such as oxygen, nitrogen, sulfur, and metals such as vanadium or nickel.
  • This charge can be constituted, in particular, by a crude oil or a heavy oil having the density indicated above.
  • the feedstock can also come from the fractionation or processing of crude oil, heavy oil, oil shale or even coal. It may thus be the residue from the distillation under reduced pressure or the residue from the distillation at atmospheric pressure of the starting materials mentioned above or, for example, the products obtained by the heat treatment of these starting materials or their distillation residues.
  • the heaviest part of the heavy hydrocarbon charges consists of a mixture of an oily phase and an asphaltic phase.
  • One way to obtain light products from the oily phase is to subject it to catalytic cracking.
  • the burden of Catalytic cracking must not, however, be too polluted by metals and not have a too high "Conradson” residue. It may be recalled that the "Conradson” residue, which gives indications on the tendency of a product to form coke, is determined according to the AFNOR NFT 60-116 standard.
  • heavy hydrocarbon feedstocks contain compounds having, in addition to hydrogen and carbon atoms, heteroatoms such as oxygen, nitrogen, sulfur and metals. Some of these compounds, in particular those containing metals, are contained in particular in the asphalt phase.
  • Asphaltenes like resins have polycyclic aromatic structures. Next to the aromatic rings are thiophenic and pyridine rings. But resins have less condensed structures than asphaltenes and lower molecular weights.
  • the compounds which precipitate by addition to the charge of a saturated aliphatic hydrocarbon having from 5 to 7 carbon atoms are generally designated under the name of asphaltenes: pentane, hexane, heptane.
  • pentane, hexane, heptane pentane, hexane, heptane.
  • a hydrocarbon with a lower boiling point for example propane.
  • this distinction is conventional and it is obvious that, if a given solvent is used at a given temperature to treat a charge, it will be possible, if the solvent and the temperature are suitable, to obtain the precipitation of asphaltene-type compounds . If the charge freed from asphaltenes is then treated with the same solvent at a higher temperature, will be able to obtain the precipitation of the resins.
  • the oily phase and the asphaltic phase are separated by the operation which consists in extracting the oily phase from the residue using a solvent.
  • This solvent can be chosen from the group consisting of: - aliphatic hydrocarbons, saturated or unsaturated, having 2 to 8 carbon atoms, alone or as a mixture. - mixtures of hydrocarbons, called distillates, having molecular weights close to those of hydrocarbons having from 2 to 8 carbon atoms, - mixtures of all the previously mentioned hydrocarbons.
  • the deasphalting can be carried out in a single step, obtaining, in this case, an oily phase and an asphaltic phase, the latter containing both the asphaltenes and the resins. It can also be done in two stages, using two different solvents and / or different operating conditions in the two stages (see, eg, US Patents No. 3,830,732 and 2,940,920). The oily phase, the resins and the asphaltenes are obtained separately, in this two-step process.
  • the Applicant has designed a deasphalting process in two stages, using, during the two stages, solvents at the same time: - relatively little different, which makes it possible to use, at least in one form of implementation, only one solvent separation installation, - sufficiently different, to obtain both: a "clean" oily phase of a quality perfectly suitable for use as a catalytic cracking charge, without additional treatment with hydrogen, - And an asphaltenes fraction, which, at room temperature, is sufficiently solid to be ground and used as solid fuel.
  • the asphaltenes fraction does not require an additional expense of flux to be used liquid.
  • the object of the present invention is therefore the preparation, in particular from a heavy hydrocarbon feedstock, of a product suitable as feedstock for a catalytic cracking.
  • the subject of the invention is a process for deasphalting a heavy hydrocarbon feed, said process leading to the obtaining: - a deasphalted oily phase having a "Conradson" index equal to or less than 10, - a "resin” fraction, - an "asphaltenes” fraction having a softening point equal to or greater than 150 ° C, said process comprising two stages of precipitation, from the charge, on the one hand, of the "asphaltenes" fraction alone, on the other hand, of the "resins” fraction, optionally in the company of the "asphaltenes” fraction, using, respectively, a heavy solvent and a light solvent, said process being characterized in that the heavy solvent and the light solvent both contain, in different proportions: - at least one hydrocarbon comprising 3 carbon atoms, - at least one hydrocarbon comprising at least 5 carbon atoms, the proportion of the hydrocarbon comprising 3 carbon atoms being higher in the light solvent than in the
  • the heavy solvent is capable of causing the "asphaltenes" fraction to precipitate, but dissolves the "resins” fraction and, a fortiori, the oily phase, -
  • the light solvent is able to precipitate the "resins” fraction and therefore, of course, the "asphaltenes" fraction, but dissolves the oily fraction.
  • the two solvents contain: - at least one hydrocarbon comprising 3 carbon atoms: propane and / or propene, - at least one hydrocarbon comprising at least 5 carbon atoms, saturated aliphatic or olefinic (including, in particular, pentane, pentene, hexane, hexene, heptane, heptene).
  • the process is therefore characterized by a search for selectivity, which leads to the combination of two solvents containing little or no hydrocarbons with 4 carbon atoms, so as to vary the selectivity according to the stage at which one is placed. .
  • Solvents can consist of a single hydrocarbon, or a mixture of hydrocarbons; thus, the heavy solvent can consist of a mixture of pentane and hexane for example.
  • hydrocarbon pentane for example
  • it may be either a well-defined hydrocarbon, such as normal pentane, or also, and this is practically always the case industrially, of a mixture of isomers of this hydrocarbon, such as, in the case of pentane, normal pentane and isopentane, essentially.
  • the light solvent contains a higher proportion than the heavy hydrocarbon solvent comprising 3 carbon atoms.
  • the heavy solvent may preferably contain from 5 to 40% by volume of hydrocarbon with 3 carbon atoms and from 60 to 95% by volume of at least one hydrocarbon with at least 5 carbon atoms.
  • the light solvent may preferably contain from 20 to 80% by volume of hydrocarbon with 3 carbon atoms and from 20 to 80% by volume of at least one hydrocarbon with at least 5 carbon atoms.
  • the method according to the invention can be implemented in two different ways.
  • the first step is the step of separation of the "asphaltenes" fraction using the heavy solvent.
  • the "resins" fraction is then precipitated using a light solvent.
  • a heavy solvent is added to the mixture of the heavy solvent, the resin fraction and the oily phase, in a second stage which is the stage of separation of the resins. as the light solvent, the latter thus resulting from the combination of the heavy solvent and said third solvent.
  • the resin fraction containing a little solvent, which is subsequently removed, - on the other hand, the oily phase in solution in the light solvent.
  • This solution is then subjected to a treatment, which makes it possible to obtain: - said third solvent, which is recycled in the second step, - A solution of the oily phase in the heavy solvent, from which it is separated in a conventional manner, the heavy solvent being recycled in the first step.
  • the treatment of the solution of the oily phase in the light solvent can in particular consist of heating said solution, preferably vaporizing the hydrocarbon comprising 3 carbon atoms.
  • the heating can be replaced by an expansion under reduced pressure of said solution.
  • the heavy solvent may preferably contain from 10 to 40% by volume of hydrocarbon with 3 carbon atoms and from 60 to 90% by volume d '' at least one hydrocarbon with at least 5 carbon atoms, and, better still, from 15 to 35% by volume of hydrocarbon with 3 carbon atoms and from 65 to 85% by volume at least one hydrocarbon with at least 5 carbon atoms.
  • the light solvent may preferably contain from 20 to 80% by volume of hydrocarbon with 3 carbon atoms and from 20 to 80% by volume. volume of at least one hydrocarbon with at least 5 carbon atoms and, better still, from 25 to 75% by volume of hydrocarbon with 3 carbon atoms and from 25 to 75% by volume of at least one hydrocarbon with at minus 5 carbon atoms.
  • the first step is a step of simultaneous precipitation of the "resin” and "asphaltene” fractions using the light solvent obtained by combining, during this step, the heavy solvent and a third solvent lighter than the desired light solvent.
  • this first step we obtain: - on the one hand, a mixture of the "resins” and “asphaltenes” fractions, - on the other hand, the oily phase in solution in the light solvent, from which it is separated later.
  • the light solvent may preferably contain from 20 to 80% by volume of hydrocarbon with 3 carbon atoms and from 20 to 80% by volume. volume of at least one hydrocarbon with at least 5 carbon atoms and, better still, from 30 to 70% by volume of at least one hydrocarbon with 3 carbon atoms and from 30 to 70% by volume of at least one hydrocarbon with at least 5 carbon atoms.
  • the heavy solvent may preferably contain from 5 to 30% by volume of hydrocarbon with 3 carbon atoms and from 70 to 95% by volume of at least one hydrocarbon with at least 5 carbon atoms and, better still, from 10 to 25% by volume of hydrocarbon with 3 carbon atoms and 75 to 90% by volume of at least one hydrocarbon with at least 5 carbon atoms.
  • the operating conditions, in the deasphalting stages, can be as follows: - pressure between 20.105 and 1.107 absolute pascals, - temperature between 100 and 300 ° C, between 1 and 10.
  • the hydrocarbon charge is introduced via line 1, into the upper part of a first extraction tower 2 heavy to deasphalt.
  • a heavy solvent the source of which will be explained later, is also introduced into the bottom of tower 2, via line 3.
  • the same heavy solvent can also be added to the feed in line 1, by a line not shown.
  • the heavy solvent of line 3 and the operating conditions of tower 2 are chosen so that only the "asphaltenes" fraction of feed 1 whose softening point is greater than or equal to 150 ° C. precipitates in said tower.
  • the pressure inside tower 2 can be between 20.105 and 1.107 absolute pascals, the temperature between 100 and 200 ° C, and the mass rate can be between 1 and 10, without these values being considered as limits.
  • the pressure can be around 40.10 5 absolute pascal, the temperatures at the bottom and at the top of tower 2 being respectively around 100 and 140 ° C, the mass ratio of heavy solvent on charge being around 2/1.
  • the "asphaltenes" fraction containing a little heavy solvent is collected at the bottom of tower 2, by line 4.
  • the charge is collected at the top of tower 2, via line 5, freed from the "asphaltenes" fraction, in solution in most of the heavy solvent introduced into tower 2.
  • the fraction collected by line 4 is conducted, after passing through at least one heater 6, in an expansion tower 7 operating, in the case of a heavy solvent C3-20 / C5-80, at a temperature of about 300 ° C and a pressure of approximately 5.105 absolute pascals. Heavy solvent is collected at the top of tower 7, via line 8, which is led, after passing through a cooler 9, into a flask 10.
  • the balloon 10 serves as storage for the heavy solvent.
  • the temperature in the flask 10 is approximately 60 ° C and the pressure approximately 5.105 absolute pascals.
  • the “asphaltenes” fraction is collected at the bottom of tower 7, via line 11, which is carried out in tower 12, operating, in the case of a heavy solvent.
  • the “asphaltenes” fraction freed from the heavy solvent, is collected at the bottom of tower 12, via line 13. This fraction can be used as solid fuel after grinding.
  • Solvent is collected at the top of tower 12, via line 19, which is led into a condenser 14.
  • the mixture of heavy solvent and filler freed from the "asphaltenes" fraction collected by line 5 is carried out in a second extraction tower 20.
  • a third solvent is introduced into this tower, via line 21, so that , in tower 20, the extraction is carried out in fact using a light solvent, resulting from the combination of the heavy solvent and the third solvent and whose proportion of hydrocarbon with 3 carbon atoms is higher than that of the heavy solvent.
  • the third solvent can be a solvent C3-40 / C5-60, that is to say containing 40% by volume of propane and 60% by volume of pentane, the light solvent then being a C3-30 / C5-70 solvent, containing 30% by volume of propane and 70% by volume of pentane.
  • the operating conditions inside tower 20 are such that the "resin" fraction precipitates.
  • the pressure inside tower 20 can be between 20.105 and 1.107 absolute pascals, the temperature between 100 and 300 ° C, the mass rate being between 1 and 10, without these values being able to be considered as limits.
  • the pressure can be approximately 40.105 absolute pascals, the temperatures at the bottom and at the top of tower 20 being approximately, respectively, 110 and 150 ° C, the mass rate being about 4/1.
  • the "resins" fraction containing a little light solvent is collected at the bottom of tower 20, through line 28.
  • the mixture of deasphalted oily phase and of light solvent collected by line 22 is led, after passage through a heater 23, in an expansion tower 24 operating, in the case of a light solvent C3-30 / C5-70, a pressure of around 25.105 absolute pascals and a temperature of around 150 ° C.
  • a pressure of around 25.105 absolute pascals and a temperature of around 150 ° C. As a result of the passage through the heater 23, part of the solvent is vaporized.
  • the hydrocarbon with 3 carbon atoms is preferably so.
  • a third solvent enriched in hydrocarbon with 3 carbon atoms is therefore collected at the top of tower 24, via line 25.
  • a third solvent C3-40 / C5-60 is thus obtained.
  • the third solvent collected by line 25 is led, after passage through a cooler 26, in a storage flask 27.
  • the temperature inside the flask 27 is about 110 ° C and the pressure about 25 bar.
  • the third solvent is then recycled via line 21 to tower 20.
  • the major part of the heavy solvent is collected at the top of the tower 32, via the line 33, which, after passing through a condenser 34, is led to the flask 10.
  • the flask 10 is connected by line 35 to line 3 and the heavy solvent can therefore be recycled to tower 2.
  • the deasphalted oily phase containing a small amount of solvent is collected at the bottom of the tower 32, via line 36, which, after passing through a heater 37, is conducted in a steam tower 38, where water vapor is introduced via line 39.
  • this tower operates at a pressure of approximately 1.5 ⁇ 105 absolute pascals and a temperature of approximately 250 ° C.
  • the deasphalted oil is collected at the bottom of the tower 38, by the line 41, and, at the top of the said tower, by the line 40, water and solvent, which are led to the condenser 14.
  • the "resins" fraction containing a little light solvent, collected by line 28 at the bottom of tower 20, is conducted, after passing through a heater 50, in an expansion tower 51 operating, in the case of a light solvent C3-30 / C5-70, at a pressure of approximately 5.105 absolute pascals and at a temperature of approximately 280 ° C.
  • the hydrocarbon charge is introduced via line 101, into the upper part of a first extraction tower 102 heavy to deasphalt.
  • a light solvent is also introduced into the bottom of tower 102, via line 103, the source of which will be explained below.
  • the "resins” and “asphaltenes” fractions precipitate.
  • the light solvent can be, for example, a C3-60 / C5-40 solvent, containing 60% by volume of propane and 40% by volume of pentane.
  • the pressure inside tower 102 can be between 20.105 and 1.107 absolute pascals, the temperature between 100 and 300 ° C, the mass rate can be between 1 and 10, without these values being considered as limits.
  • the pressure can be around 40.105 absolute pascals, the temperatures at the bottom and at the top of tower 102 being around 100 and 130 ° C, respectively, the mass rate being about 2/1.
  • the solvent and the operating conditions of tower 109 are chosen so that only the "asphaltenes" fraction of line 105 whose softening point is greater than or equal to 150 ° C. precipitates in said tower.
  • the heavy solvent can be a C3-20 / C5-80 solvent, the solvent in line 106 being a C3-10 / C5-90 solvent.
  • the pressure inside tower 109 can be between 20.105 and 1.105 absolute pascals, the temperature between 100 and 200 ° C, the mass rate can be between 1 and 10, without these values being considered as limits.
  • the pressure can be around 40.105 absolute pascals, the temperatures at the bottom and at the top of tower 109 being respectively about 100 and 140 ° C, the mass ratio of heavy solvent on charge of tower 102 being approximately 2/1.
  • the "asphaltenes" fraction containing a little heavy solvent is collected at the bottom of tower 109, via line 110.
  • the major part of the solvent is collected at the top of the tower 119, via the line 120, which, after passing through a condenser 121, is led to the flask 122.
  • the flask 122 is connected by line 123 to line 106 and the solvent can therefore be recycled.
  • this tower operates at a pressure of approximately 1.5 ⁇ 105 absolute pascals and a temperature of approximately 280 ° C.
  • the "resins” are collected at the bottom of the tower 126, by the line 128, and at the top of the said tower, by the line 129, water and solvent, which are led to the condenser 14 ⁇ .
  • a mixture of deasphalted oil and light solvent is collected at the top of the tower 102, via the line 129, which, after passing through a heater 131, is led into an expansion tower 132 operating, in the case of a light solvent C3-60 / C5-40, at a pressure of approximately 25.105 absolute pascals and a temperature of approximately 140 ° C.
  • the major part of the light solvent is collected at the top of tower 132, by line 133, which is recycled to line 103 by line 114 and the refrigerant 115.
  • the deasphalted oily phase containing a little solvent is collected at the bottom of tower 132, via line 134, which, after passing through a heater 135, is carried out in a tower 136 for driving with steam, where water vapor is introduced via line 137.
  • this tower operates at a pressure of approximately 1.5.105 absolute pascals and a temperature of approximately 250 ° C.
  • the deasphalted oil is collected at the bottom of the tower 136, by the line 138, and, at the top of the said tower, by the line 139, water and solvent, which are led to the condenser 14 ⁇ .
  • FIG. 3 represents a variant of FIG. 1, in which the separation of the light solvent from the deasphalted oil is carried out in such a way that the light solvent contains even more hydrocarbon with 3 carbon atoms.
  • the separation of the resins from the oil is better and makes it possible to obtain an even deasphalted oil. "clean", that is to say having an even lower "Conradson” residue.
  • the mixture of heavy solvent C3-20 / C5-80 and of filler no longer containing "asphaltenes" collected by line 5 is led into a second extraction tower 200.
  • line 210 is introduced, a third solvent C3-50 / C5-50, the extraction being carried out in fact using a light solvent C3-35 / C5-65.
  • the pressure in the tower can be around 40.105 absolute pascals, the temperatures at the bottom and at the top of the tower 200 being around, respectively, 115 and 145 ° C, the mass rate being about 4/1.
  • the mixture of deasphalted oily phase and of light solvent C5-35 / C5-65 is collected at the top of tower 200, via line 220.
  • Tower 240 is equipped with three rackings.
  • a mixture of deasphalted oil and solvent C3-20 / C5-80 which, after passing through an expansion valve 300, where its pressure and its temperature are lowered, respectively , at 5.105 absolute pascals and 95 ° C, and passage through a heater 310, is led in a pressure reduction tower 320 operating at a pressure of 5.105 absolute pascals and a temperature of approximately 120 ° C, -
  • a lateral withdrawal 500 a solvent C3-30 / C5-70, part of which is taken to line 33, the other part being recycled to tower 240 by line 510, after passage through a coolant 520; -
  • a C3-50 / C550 solvent which, after passing through a coolant 260, is led into a storage flask 270, this solvent then
  • Tower 320 is equipped with three withdrawals: - At the top of this tower, there is collected, via line 528, solvent C3-50 / C5-50, which is recycled to line 250; - A C3-15 / C5-85 solvent is collected by a lateral withdrawal 530, part of which is taken to line 33, while the other part is recycled to tower 320, via line 550, after passing through a refrigerant 540; - The deasphalted oily phase containing a little solvent is collected at the bottom of tower 320, via line 360.
  • this phase after passing through a heater 370, is carried out in a water vapor drive tower 380, where water vapor is introduced via line 390.
  • deasphalted oil is collected by line 410 and, at the top of said tower, by line 400, water and solvent, which are led to condenser 14.
  • the process according to the invention is particularly useful, as the following examples show, for the simultaneous preparation of a deasphalted oil, suitable as a catalytic cracking charge, having a "Conradson" residue less than or equal to 10, preferably less than or equal to 9 and, better still, less than or equal to 8, and of an "asphaltenes" fraction, having a softening point equal to or greater than 150 ° C, preferably equal to or greater than 160 ° C and, better still, equal to or greater than 170 ° C.
  • This example relates to the treatment of a hydrocarbon feedstock constituted by the residue from the distillation under reduced pressure of the residue from the distillation under atmospheric pressure of a crude oil of Safaniya origin.
  • the characteristics of this charge are as follows: - density at 15 ° C (measured according to AFNOR NFT 60-101 standard): 1035 kg / m3, - viscosity at 100 ° C (measured according to AFNOR NFT 60-100 standard): 0.56.
  • This charge is treated in a unit implementing the method according to the invention of the type presented in FIG. 1.
  • Solvents C3-C5 are used in the unit, the compositions of which are given in Table I below.
  • This example relates to the treatment of a hydrocarbon feedstock constituted by the residue from the distillation under atmospheric pressure of the visbreaking effluent from a residue from the distillation under reduced pressure of a SAFANIYA crude oil.
  • the characteristics of this charge are as follows: - density at 15 ° C (measured according to AFNOR NFT 60-101 standard): 1,060 kg / m3, - viscosity at 100 ° C (measured according to AFNOR NFT 60-100 standard): 0.17.10 ⁇ 2 m2 / s, - "Conradson" residue (measured according to AFNOR NFT 60-116 standard): 27% by weight, - content of: * asphaltenes (measured according to AFNOR NFT 60-115 standard): 22% by weight, * sulfur (measured by X-ray fluorescence): 6.2% by weight, * nickel (measured by X-ray fluorescence): 53 ppm, * vanadium (measured by X-ray fluorescence): 175 ppm
  • This load is treated in a unit implementing the method according to the invention of the type shown in FIG. 1.
  • Solvents C3-C5 are used in the unit with compositions identical to those of the solvents of Example 1.
  • This example relates to the treatment of a hydrocarbon feedstock constituted by the residue of the distillation under reduced pressure of the residue of the distillation under atmospheric pressure of a crude oil of Iraq origin.
  • the characteristics of this charge are as follows: - density at 15 ° C (measured according to AFNOR NFT 60-101 standard): 1016 kg / m3, - viscosity at 100 ° C (measured according to AFNOR NFT 60-100): 900 10 ⁇ 6 m2 / s - "Conradson" residue (measured according to AFNOR NFT 60-116): 17% by weight, - content of: * asphaltenes (measured according to AFNOR NFT 60-115 standard): 6% by weight, * sulfur (measured by X-ray fluorescence): 4.9% by weight, * nickel (measured by X-ray fluorescence): 43 ppm, * vanadium (measured by X-ray fluorescence): 102 ppm
  • This load is treated in a unit implementing the method according to the invention of the type shown in FIG. 1.
  • Solvents C3-C6 are used in the unit, the compositions of which are given in Table VIII below.
  • This example concerns the treatment of a hydrocarbon feedstock constituted by the residue from the distillation under reduced pressure of the residue from the distillation under atmospheric pressure of a crude oil of SAFANIYA origin.
  • the characteristics of this load are as follows: - density at 15 ° C (measured according to AFNOR NFT 60-101 standard): 1035 kg / m3, - viscosity at 100 ° C (measured according to AFNOR NFT 60-100): 5,600 10 ⁇ 6 m2 / s - "Conradson" residue (measured according to AFNOR NFT 60-116 standard): 23% by weight, - content of: * asphaltenes (measured according to standard AFNOR NFT 60-115): 16% by weight, * sulfur (measured by X-ray fluorescence): 5.5% by weight, * nickel (measured by X-ray fluorescence): 43 ppm, * vanadium (measured by X-ray fluorescence): 138 ppm
  • This charge is treated in a unit implementing the method according to the invention of the type presented in FIG. 2.
  • Solvents C3-C5 are used in the unit, the compositions of which are given in Table XII below.

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  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
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  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP87401091A 1986-05-15 1987-05-14 Verfahren zur Entfernung von Asphalt aus einer Kohlenwasserstoffbeschickung Expired - Lifetime EP0246956B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8606994 1986-05-15
FR8606994A FR2598716B1 (fr) 1986-05-15 1986-05-15 Procede de desasphaltage d'une charge hydrocarbonee lourde

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EP0246956A1 true EP0246956A1 (de) 1987-11-25
EP0246956B1 EP0246956B1 (de) 1990-11-28

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US (1) US4810367A (de)
EP (1) EP0246956B1 (de)
JP (1) JP2525409B2 (de)
CA (1) CA1330063C (de)
DE (1) DE3766415D1 (de)
FR (1) FR2598716B1 (de)

Cited By (4)

* Cited by examiner, † Cited by third party
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WO1990010048A1 (en) * 1989-02-27 1990-09-07 Kerr-Mcgee Corporation Solvent extraction process
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WO2000046164A1 (en) * 1999-02-02 2000-08-10 Shell Internationale Research Maatschappij B.V. Solid-state composition comprising solid particles and binder
US6749678B1 (en) 1999-02-02 2004-06-15 Shell Oil Company Solid-state composition comprising solid particles and binder
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FR2939804A1 (fr) * 2008-12-11 2010-06-18 Total Raffinage Marketing Procede de valorisation de bruts lourds et de residus petroliers.

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EP0246956B1 (de) 1990-11-28
FR2598716A1 (fr) 1987-11-20
JP2525409B2 (ja) 1996-08-21
JPS62273289A (ja) 1987-11-27
FR2598716B1 (fr) 1988-10-21
US4810367A (en) 1989-03-07
DE3766415D1 (de) 1991-01-10
CA1330063C (fr) 1994-06-07

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