US20040069685A1 - Method of refining petroleum - Google Patents

Method of refining petroleum Download PDF

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Publication number
US20040069685A1
US20040069685A1 US10/432,826 US43282603A US2004069685A1 US 20040069685 A1 US20040069685 A1 US 20040069685A1 US 43282603 A US43282603 A US 43282603A US 2004069685 A1 US2004069685 A1 US 2004069685A1
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Prior art keywords
oil
vacuum
residue
feed
deasphalted
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Inventor
Makoto Inomata
Yasushi Fujimura
Tsuyoshi Okada
Kozo Imura
Hajime Sasaki
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JGC Corp
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JGC Corp
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Assigned to JGC CORPORATION reassignment JGC CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FUJIMURA, YASUSHI, IMURA, KOZO, INOMATA, MAKOTO, OKADA, TSUYOSHI, SASAKI, HAJIME
Publication of US20040069685A1 publication Critical patent/US20040069685A1/en
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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
    • C10G67/16—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural parallel stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/14—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
    • C10G65/16—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only including only refining steps
    • 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 present invention relates to an oil refining method for producing a plurality of oil products of high added value with a high efficiency, and more particularly, to an oil refining method for producing a plurality of oil products of high added value that have different specifications with a high efficiency from a heavy feed oil or a low sulfur oil.
  • SDA solvent deasphalting
  • VDU vacuum distillation
  • VGO vacuum gas oil
  • Fuels for transportation such as gasoline and gas oil can be produced by separating deasphalted oil and vacuum gas oil from ultra heavy crude that is found in vast amount of reserves or atmospheric residue of which an over supply is expected in the future, and processing the deasphalted oil or vacuum gas oil by fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • An object of the present invention is to provide a method of refining oil for producing oil products (for example, gas turbine fuel) that includes a vanadium (V) content of 0.5 wt ppm or lower and intermediate oil products having metal content (V+Ni) of 30 wt ppm or lower that can be used as the feed for a fluid catalytic cracking (FCC) or a hydrocracking (HCR) process efficiently at the same time, whether a particularly heavy feed oil or a feed oil having a low sulfur content is used as the starting material.
  • oil products for example, gas turbine fuel
  • V vanadium
  • V+Ni intermediate oil products having metal content
  • a method for refining oil according to the first aspect of the present invention is a method for producing oil products including a plurality of intermediate oil products by refining a feed oil, comprising a fractional distillation process for separating the feed oil into distillate and a residue through distillation; a hydrorefining process wherein at least a part of the distillate obtained in the fractional distillation process is refined and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain a hydrorefined oil; a solvent deasphalting process wherein the residue is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein at least a part of the deasphalted oil is demetalized and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized; and a first mixing
  • the yield of deasphalted oil produced in the solvent deasphalting process can be improved by producing the gas turbine fuel and the feed for a fluid catalytic cracking or a hydrocracking process at the same time, thereby suppressing the production of asphaltene (pitch) from the atmospheric residue.
  • a method for refining oil according to the second aspect of the present invention comprises a fractional distillation process for separating the feed oil into a distillate and a residue through distillation; a hydrorefining process wherein at least a part of the distillate obtained in the fractional distillation process is refined and desulfurized through hydrogenation in the presence of hydrogen and a catalyst thereby to obtain a hydrorefined oil; a solvent deasphalting process wherein the residue is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein at least a part of the deasphalted oil is demetalized and desulfurized through hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized; a vacuum fractional distillation process wherein the HDMS refined oil is distilled in a vacuum and separated into vacuum gas oil and vacuum
  • the HDMS refined oil is subjected to a vacuum fractional distillation process to be separated into vacuum gas oil and vacuum residue having low metal content and residual carbon content by making use of the range of boiling points of the distillation properties particularly in the vacuum fractional distillation process, relatively high concentrations of vanadium and metals can be allowed for the HDMS refined oil, thus improving the yield of deasphalted oil in the solvent deasphalting process, and therefore it is possible to suppress the production of asphaltene (pitch) from the atmospheric residue.
  • a method for refining oil according to the third aspect of the present invention comprises a fractional distillation process for separating the feed oil into distillate and a residue through distillation; a hydrorefining process wherein at least a part of the distillate obtained in the fractional distillation process is refined and desulfurized through hydrogenation in the presence of hydrogen and a catalyst thereby to obtain a hydrorefined oil; a vacuum fractional distillation process wherein the residue is distilled in a vacuum and separated into vacuum gas oil and vacuum residue; a solvent deasphalting process wherein the vacuum residue is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein the vacuum gas oil and deasphalted oil are mixed and the mixture is subjected to hydrodemetalizating/desulfurizing process in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that is demetalized and des
  • the intermediate oil product used as the feed for a fluid catalytic cracking or a hydrocracking process has a higher tolerable concentrations of metal contents than those of gas turbine fuel or the like, the yield of the deasphalted oil in the solvent deasphalting process can be improved by producing the gas turbine fuel and the feed for a fluid catalytic cracking or a hydrocracking process at the same time, thereby suppressing the production of asphaltene (pitch) from the atmospheric residue.
  • the amount of pitch produced can be made lower than in the prior art, in which a large quantity of pitch that has a low commodity value generated as a byproduct, and the yield of producing a plurality of oil products having a high added values is improved, thus resulting in a greatly improved productivity.
  • a method for refining oil according to the fourth aspect of the present invention is a method for producing oil products including a plurality of intermediate oil products by refining a feed oil that includes low sulfur content, and comprises a fractional distillation process for separating the feed oil into distillate and a residue through distillation; a solvent deasphalting process wherein the residue obtained in the fractional distillation process is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein at least a part of the deasphalted oil is demetalized and desulfurized through hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized; and a fourth mixing process wherein a part of the HDMS refined oil and at least a part of the distillate are mixed thereby to produce one of the oil products.
  • the intermediate oil product used as the feed for a fluid catalytic cracking or a hydrocracking process has a higher tolerable concentrations of metal contents than that of gas turbine fuel or the like, the yield of deasphalted oil produced in the solvent deasphalting process can be improved by producing the gas turbine fuel and the feed for a fluid catalytic cracking or a hydrocracking process at the same time, thereby suppressing the production of asphaltene (pitch) from the atmospheric residue.
  • a oil refining method comprises a fractional distillation process for separating the feed oil into distillate and a residue through distillation; a solvent deasphalting process wherein the residue obtained in the fractional distillation process is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein at least a part of the deasphalted oil is demetalized and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized; a vacuum fractional distillation process wherein the HDMS refined oil is distilled in a vacuum and separated into vacuum gas oil and vacuum residue; and a fifth mixing process wherein at least a part of the vacuum gas oil and at least a part of the distillate are mixed in order to produce one of the oil products.
  • the HDMS refined oil is subjected to vacuum distillation so as to separate into vacuum gas oil and vacuum residue having low metal content and residual carbon content by making use of the range of boiling points of the distillation properties particularly in the vacuum fractional distillation process, thus relatively high concentrations of vanadium and metals can be allowed for the HDMS refined oil, thereby improving the yield of deasphalted oil in the solvent deasphalting process, and therefore it is possible to suppress the production of asphaltene (pitch) from the atmospheric residue.
  • a oil refining method of the sixth aspect of the present invention comprises a fractional distillation process for separating the feed oil into distillate and a residue through distillation; a vacuum fractional distillation process wherein the residue obtained in the fractional distillation process is distilled in a vacuum and separated into vacuum gas oil and vacuum residue; a solvent deasphalting process wherein the vacuum residue is deasphalted with a solvent thereby to obtain deasphalted oil as an extract and asphaltene (pitch) as the residue; a hydrodemetalizating/desulfurizing process wherein the vacuum gas oil and the deasphalted oil are mixed and the mixture is demetalized and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized; and a sixth mixing process wherein a part of the HDMS refined oil and at least a part of the distillate are mixed thereby to produce one of the oil products.
  • the vanadium (V) content of the mixed oil becomes sufficiently low and it is possible to obtain an oil product that can be used as gas turbine fuel. It is also possible to produce an intermediate oil product having sufficiently low metal content (V+Ni) that can be used as the feed for a fluid catalytic cracking or a hydrocracking process even from the remainder of HDMS refined oil that is obtained by processing the mixture of vacuum gas oil and deasphalted oil in the hydrodemetalizating/desulfurizing process.
  • the intermediate oil product used as the feed for a fluid catalytic cracking or a hydrocracking process has a higher tolerable concentration of metal contents than that of gas turbine fuel or the like, the yield of deasphalted oil produced in the solvent deasphalting process can be improved by producing the gas turbine fuel and the feed for a fluid catalytic cracking or a hydrocracking process at the same time, thereby suppressing the production of asphaltene (pitch) from the vacuum residue.
  • FIG. 1 through FIG. 6 are process flow diagrams explaining the first through sixth embodiments of the oil refining method according to the present invention.
  • FIG. 7 through FIG. 12 are process flow diagrams explaining the oil refining methods of the first through sixth experimental examples.
  • FIG. 1 is a process flow diagram explaining an embodiment of the oil refining method according to the present invention, wherein a heavy crude oil is used as feed oil from which gas turbine fuel (GTF) and a feed for fluid catalytic cracking (FCC) process or a feed for hydrocracking (HCR) process are produced at the same time.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • feed oil to be processed there is no limitation to the feed oil to be processed, and any hydrocarbon oil ranging from crude oil to heavy oil can be used.
  • the description that follows will deal with cases where the present invention is applied to heavy crude oil such as Orinoco tar, particularly to heavy oils having an API gravity not higher than 20 while achieving a remarkable effect of improving the yield of producing a plurality of oil products having a high added values.
  • API gravity is an index for classifying crude oils by the physical properties thereof, and is calculated from the specific gravity by the following formula, where S is the specific gravity at 60 degrees Fahrenheit.
  • API (141.5 /S ) ⁇ 131.5
  • the feed oil is first subjected to fractional distillation process 1 to separate into a distillate M1 consisting of low-boiling point oil and a residue M2 of high boiling point by distilling similarly to the prior art.
  • fractional distillation process 1 is preferably used as the fractional distillation apparatus of this example, there is no limitation to the apparatus as long as it is means for fractional distillation.
  • Distillates may be either collectively recovered without classifying, or recovered individually after classifying by the boiling point. In case distillates are recovered in a plurality of classes and some class of the distillate satisfies the specification requirements for petroleum, the hydrorefining process 2 that would follow may be omitted or bypassed as indicated by arrow 11 .
  • distillate M1 obtained in the fractional distillation process 1 is introduced into the hydrorefining process (HT process) 2 to be refined and desulfurized by hydrogenation in the presence of hydrogen and a catalyst, thereby producing hydrorefined oils M3, M3′.
  • HT process hydrorefining process
  • the residue M2 obtained in the fractional distillation process 1 is introduced into the solvent deasphalting process (SDA process) 3 to be deasphalted with a solvent, thereby to obtain deasphalted oil (DAO) M4 as an extract and asphaltene (pitch) M5.
  • SDA process solvent deasphalting process
  • DAO deasphalted oil
  • pitch asphaltene
  • the residue M2 is put into contact with the solvent in counterflow in a solvent extraction tower and is separated into deasphalted oil and asphaltene (pitch) that includes metals and residual carbon in high concentrations.
  • the deasphalted oil is recovered together with the solvent through the top of the tower, and the solvent is separated from the recovered material in super-critical state.
  • Asphaltene (pitch) is recovered together with the solvent through the bottom of the tower, and the solvent in the recovered material is removed by evaporation.
  • the extraction ratio of deasphalted oil from the feed oil varies among components included in the deasphalted oil such as sulfur, vanadium, nitrogen and residual carbon.
  • the extraction ratio for the vanadium content included in the deasphalted oil to the vanadium content included in the feed oil is preferably controlled to within 20% when the atmosphere distilled residue is used as the feed oil, or within 15% when the vacuum distilled residue is used as the feed oil.
  • the extraction ratio may be in a range appropriately selected in accordance to the type of feed oil and the vanadium content.
  • the vanadium content included in the deasphalted oil is preferably controlled to within 25 wt ppm when atmosphere distilled residue is used as the feed oil, or within 70 wt ppm when vacuum distilled residue is used as the feed oil.
  • refined oil can be produced efficiently with the extraction ratio in the solvent deasphalting process being maximized, without placing a significant load on the hydrodemetalizating/desulfurizing process that follows the solvent deasphalting process, in either of the cases described above.
  • the refining process that follows the solvent deasphalting process 3 includes only the hydrodemetalizating/desulfurizing process 4 , it is preferable to control the extraction rate of the solvent deasphalting process 3 so that the extraction ratio for the vanadium content included in the deasphalted oil M4 to the vanadium (V) content included in the residue M2 used as the feed oil is 20% or lower.
  • At least a part of the deasphalted oil M4 obtained in the solvent deasphalting process 3 is introduced into the hydrodemetalizating/desulfurizing process (HDMS process) 4 , wherein the deasphalted oil is demetalized and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain HDMS refined oil that has been demetalized and desulfurized.
  • the hydrodemetalizating/desulfurizing process is basically the same as the hydrorefining process 2 described previously, and the description thereof will be omitted.
  • the demetalizing and desulfurizing conditions for the HDMS refined oil M6 obtained in the hydrodemetalizating/desulfurizing process are preferably selected so as to achieve the vanadium (V) content of 2 wt ppm or lower, preferably 1 wt ppm or lower, and a sulfur content of 0.5 wt % or lower, preferably 0.3 wt % or lower.
  • mixing condition is set so as to achieve the vanadium (V) content of 0.5 wt ppm or lower.
  • V vanadium
  • rate of the HDMS refined oil M6 to the hydrorefined oil M3 is set to 1:1 or less (that is, a smaller proportion of the HDMS refined oil M6) in volume proportion for mixing, with the vanadium content in the hydrorefined oil M3 being set to 0 wt ppm.
  • the remainder that is not subjected to the first mixing process 5 is used as an intermediate oil product to be used as the feed for the fluid catalytic cracking (FCC) process or the hydrocracking (HCR) process.
  • the hydrorefined oil M3 the remainder that is not subjected to the first mixing process 5 may be used as oil product M3′ such as naphtha, gasoline, kerosene, or gas oil.
  • the intermediate oil product used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process has a higher tolerable concentrations of metal contents than that of gas turbine fuel (GTF) or the like, the yield of deasphalted oil M4 produced in the solvent deasphalting process 3 can be improved without accompanying a load of hydrodemetalizating/desulfurizing process, thereby suppressing the production of asphaltene (pitch) M5 from the residue M2.
  • FIG. 2 is a process flow diagram explaining the second embodiment of the oil refining method according to the present invention, wherein gas turbine fuel (GTF) and feed for fluid catalytic cracking (FCC) process or feed for hydrocracking (HCR) process are produced at the same time from a feed oil, similarly to the first embodiment shown in FIG. 1.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the second embodiment is different from the first embodiment shown in FIG. 1 mainly in that a vacuum fractional distillation process 6 is provided to follow the hydrodemetalizating/desulfurizing process 4 , so as to process the HDMS refined oil M6 that has been obtained in a vacuum distillation and separate it into vacuum gas oil M7 and vacuum residue M8 through a vacuum distillation process.
  • a vacuum fractional distillation process 6 is provided to follow the hydrodemetalizating/desulfurizing process 4 , so as to process the HDMS refined oil M6 that has been obtained in a vacuum distillation and separate it into vacuum gas oil M7 and vacuum residue M8 through a vacuum distillation process.
  • the HDMS refined oil M6 obtained similarly to the example shown in FIG. 1 is distilled in a vacuum in the vacuum fractional distillation process 6 .
  • the HDMS refined oil M6 is introduced into a vacuum distillation tower where the HDMS refined oil M6 is distilled and separated into a low-boiling point component and a high-boiling point component, while the vacuum gas oil M7 having low boiling point is obtained from the top of the tower and the vacuum residue M8 having a high boiling point is obtained from the bottom of the tower.
  • the demetalizing and desulfurizing conditions for the HDMS refined oil M6 obtained by hydrodemetalizating/desulfurizing process of the deasphalted oil M4 are selected so as to control the vanadium (V) content of the HDMS refined oil M6 to 20 wt ppm or lower, preferably 10 wt ppm or lower, and the sulfur content is desirably controlled to 0.5 wt % or lower, preferably 0.3 wt % or lower.
  • the mixing condition is set so as to achieve the vanadium (V) content of 0.5 wt ppm or lower similarly to the example shown in FIG. 1.
  • the mix proportion is properly adjusted according to the vanadium content of the vacuum gas oil M7 similarly to the previous example.
  • vanadium (V) content of the vacuum gas oil M7 is 0.5 wt ppm or lower, this may be used as gas turbine fuel (GTF) without adding the hydrorefined oil M3 thereto.
  • the remainder of the vacuum gas oil M7, the vacuum residue M8 obtained by vacuum distillation, and remainder of the HDMS refined oil M6 that is not fed to the vacuum fractional distillation process 6 are used individually or in an appropriate combination thereof thereby to provide an intermediate oil product used as the feed for fluid catalytic cracking (FCC) process or the feed for hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • a part of the M4 may be introduced into the bypass 12 to be mixed with a part of the vacuum residue M8 sent from the vacuum fractional distillation process 6 , instead of being subjected to the hydrodemetalizating/desulfurizing process 4 , thereby to produce intermediate oil products used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the HDMS refined oil M6 obtained in the hydrodemetalizating/desulfurizing process 4 may also be introduced into the bypass 12 to be mixed with the vacuum residue M8 sent from the vacuum fractional distillation process 6 thereby to produce intermediate oil products used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • FIG. 3 is a process flow diagram explaining the third embodiment of the present invention, wherein gas turbine fuel (GTF) and feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process are produced at the same time from a feed oil, similarly to the example shown in FIG. 1.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the third embodiment is different from the first embodiment shown in FIG. 1 mainly in that fractional distillation process 1 is followed by a vacuum fractional distillation process 20 wherein the residue M2 is separated into vacuum gas oil M11 and vacuum residue M12 by vacuum distillation, a solvent deasphalting process 21 wherein the vacuum residue M12 is separated into deasphalted oil M13 and asphaltene (pitch) M14 by solvent deasphalting, and a hydrodemetalizating/desulfurizing process 22 wherein a mixture of the deasphalted oil M13 and the vacuum gas oil M11 is subjected to hydrodemetalizating/desulfurizing process thereby to produce HDMS refined oil M15 .
  • the residue M2 is introduced into a vacuum distillation tower where the residue M2 is distilled and separated into a low-boiling point component and a high-boiling point component, while the vacuum gas oil M11 having the lower boiling point is obtained from the top of the tower and the vacuum residue M12 having the higher boiling point is obtained from the bottom of the tower.
  • the vacuum residue M12 thus obtained is subjected to the solvent deasphalting process 21 and is separated into deasphalted oil M13 and asphaltene (pitch) M14 .
  • the solvent deasphalting process is similar to those in the examples shown in FIG. 1 and FIG. 2, the desirable upper limit of the extraction ratio of vanadium for the deasphalted oil M13 obtained from the vacuum residue by solvent deasphalting process becomes lower in correspondence to the concentrations of metals, residual carbon and sulfur that are higher than those of the residue M2, and therefore the extraction ratio is preferably controlled to 15%.
  • the demetalizing and desulfurizing conditions for the HDMS refined oil M15 thus obtained are preferably selected so as to achieve the vanadium (V) content of 2 wt ppm or lower, preferably 1 wt ppm or lower, and a sulfur content of 0.5 wt ppm or lower, preferably 0.3 wt ppm or lower.
  • the remainder that is not subjected to the third mixing process 23 may be used as an intermediate oil product to be fed to fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the M13 and the M11 may be, instead of being mixed, subjected to hydrodemetalizating/desulfurizing process in separate reactors each under optimum conditions, and then mixed or at least part of the vacuum gas oil M11 that has been subjected to hydrodemetalizating/desulfurizing process and at least a part of the hydrorefined oil M3 may be mixed thereby to obtain gas turbine fuel (GTF) that has vanadium (V) content of 0.5 wt ppm or lower.
  • GTF gas turbine fuel
  • V vanadium
  • the intermediate oil product used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process has a higher tolerable concentrations of metal contents than that of gas turbine fuel (GTF) or the like, the yield of deasphalted oil M13 in the solvent deasphalting process 21 can be improved by producing the gas turbine fuel and the feed for a fluid catalytic cracking or a hydrocracking process at the same time, thereby suppressing the production of asphaltene (pitch) M14 from the vacuum residue M12 .
  • the low-sulfur crude in this specification refers to crude oil such as Arabian Light, Egyptian Light, Egyptian Heavy, Marban, and other crude oil that includes sulfur content in a concentration similar to or lower than those of the former species, specifically crude oils including a sulfur content of 2.0 wt % or lower.
  • HT process 2 of the first embodiment that deals with heavy crude oil is omitted in the following embodiments because low-sulfur crude is used.
  • basically the same processes as those of the first embodiment are carried out.
  • processes identical to those of the first embodiment will be indicated by adding a letter A to the end of the reference numeral used in the first embodiment.
  • FIG. 4 is a process flow diagram showing the fourth embodiment of the present invention.
  • the low-sulfur crude mentioned above is used as the feed oil which is subjected to a fractional distillation process 1 A and is distilled similarly to the prior art so as to be separated into a distillate M1A consisting of low-boiling point oil and a residue M2A having a higher boiling point.
  • An apparatus similar to that of the first embodiment may be used.
  • the distillate M1A obtained in the fractional distillation process 1 A is separated into distillates M3 A, M3 A′ by a flasher 30 .
  • the residue M2A obtained in the fractional distillation process 1 A is deasphalted with a solvent in a solvent deasphalting process (SDA process) 3 A, thereby to obtain deasphalted oil (DAO) M4A as an extract and asphaltene (pitch) M5A.
  • SDA process solvent deasphalting process
  • the residue 2 A is put into contact with the solvent in counterflow in a solvent extraction tower and is separated into deasphalted oil and asphaltene (pitch) that includes metal and residual carbon in high concentrations.
  • the deasphalted oil is recovered together with the solvent through the top of the tower, and the solvent is separated from the recovered material in super-critical state.
  • Asphaltene (pitch) is recovered together with the solvent through the bottom of the tower, and the solvent in the recovered material is removed by evaporation.
  • At least a part of the deasphalted oil M4A obtained in the solvent deasphalting process 3 A is introduced into the hydrodemetalizating/desulfurizing process (HDMS process) 4 A, so that the part of the deasphalted oil is demetalized and desulfurized by hydrogenation in the presence of hydrogen and a catalyst thereby to obtain the HDMS refined oil M6A that has been demetalized and desulfurized.
  • the hydrodemetalizating/desulfurizing process is basically the same as the hydrorefining process that deals with heavy crude oil described previously, and the description thereof will be omitted.
  • Hydrodemetalizing and desulfurizing conditions are preferably selected so as to obtain the HDMS refined oil M6A having vanadium (V) content of 2 wt ppm or lower, preferably 1 wt ppm or lower, and a sulfur content of 0.5 wt % or lower, preferably 0.3 wt % or lower.
  • V vanadium
  • a part of the HDMS refined oil M6A obtained in the hydrodemetalizating/desulfurizing process 4 A and at least a part of the distillate M3 A are mixed in the fourth mixing process 5 A thereby to obtain a petroleum product.
  • the mix proportion is set so as to achieve a vanadium (V) content of 0.5 wt ppm or lower in the petroleum product.
  • V vanadium
  • rate of the HDMS refined oil M6A to the distillate M3 A is set to 1:1 or less (that is, the smaller proportion of the HDMS refined oil M6A) in volume proportion for mixing.
  • the remainder thereof that is not subjected to the fourth mixing process 5 A is used as an intermediate oil product to be fed to the fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the hydrorefined oil M3 the remainder thereof that is not subjected to the first mixing process 5 A may be used as an oil product M3 A′ such as naphtha, gasoline, kerosene or gas oil.
  • the intermediate oil product used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process has a higher tolerable concentrations of metal contents than that of gas turbine fuel (GTF) or the like, the yield of deasphalted oil M4A produced in the solvent deasphalting process 3 A can be improved without accompanying load of hydrodemetalizating/desulfurizing process, thereby suppressing the production of asphaltene (pitch) M5A from the residue M2A.
  • FIG. 5 is a process flow diagram explaining the fifth embodiment of the oil refining method according to the present invention, in which gas turbine fuel (GTF) and feed for fluid catalytic cracking (FCC) process or feed for hydrocracking (HCR) process are produced at the same time from a feed oil, similarly to the embodiment shown in FIG. 4.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • This embodiment is different from the embodiment shown in FIG. 4 mainly in that vacuum fractional distillation process 6 A is provided to follow the hydrodemetalizating/desulfurizing process 4 A, so as to process the HDMS refined oil M6A in a vacuum distillation and separate it into vacuum gas oil M7A and vacuum residue M8A.
  • the HDMS refined oil M6A obtained similarly to the example shown in FIG. 4 is distilled in a vacuum in the vacuum fractional distillation process 6 A.
  • the HDMS refined oil M6A is introduced into a vacuum distillation tower where the HDMS refined oil M6A is distilled and separated into a low-boiling point component and a high-boiling point component, while the vacuum gas oil M7A having the lower boiling point is obtained from the top of the tower and the vacuum residue M8A having the higher boiling point is obtained from the bottom of the tower.
  • extraction ratio of the deasphalted oil M4A obtained in the solvent deasphalting process can be controlled so that desirable upper limit of the vanadium (V) content is set to, for example, 50 wt ppm.
  • V vanadium
  • the demetalizing and desulfurizing conditions for the HDMS refined oil M6A obtained from the deasphalted oil M4A through the hydrodemetalizating/desulfurizing process are preferably selected so as to achieve the vanadium (V) content of 20 wt ppm or lower, preferably 10 wt ppm or lower, while the sulfur content is desirably set to 0.5 wt % or lower, preferably 0.3 wt % or lower.
  • vanadium (V) content is controlled to 0.5 wt ppm or lower similarly to the example shown in FIG. 4. In that case, the mix proportion is adjusted according to the vanadium content of the vacuum gas oil M7A similarly to the previous example.
  • vanadium (V) content of the vacuum gas oil M7A is 0.5 wt ppm or lower, this may be used as gas turbine fuel (GTF) without adding the distillate M3 A.
  • the remainder of the vacuum gas oil M7A, the vacuum residue M8A obtained by vacuum distillation and remainder of the HDMS refined oil M6A that is not fed to the vacuum fractional distillation process 6 A are used individually or in an appropriate combination thereof as an intermediate oil product to be used as the feed for fluid catalytic cracking (FCC) process or the feed for hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the HDMS refined oil M6A obtained in the hydrodemetalizating/desulfurizing process 4 A may also be introduced into the bypass 12 A to be mixed with the vacuum residue M8A sent from the vacuum fractional distillation process 6 A thereby to produce intermediate oil products used as the feed for fluid catalytic cracking (FCC) or hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • FIG. 6 is a process flow diagram explaining the sixth embodiment of the oil refining method according to the present invention, for a case of producing gas turbine fuel (GTF) and feed for fluid catalytic cracking (FCC) process or feed for hydrocracking (HCR) process at the same time from a feed oil, similarly to the embodiment shown in FIG. 4.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • This embodiment is different from the embodiment shown in FIG. 4 mainly in that the fractional distillation process 1 A is followed by a vacuum fractional distillation process 20 A wherein the residue M2A is separated into vacuum gas oil M11 A and vacuum residue M12 A by vacuum distillation, a solvent deasphalting process 21 A wherein the vacuum residue M12 A is separated into deasphalted oil M13 A and asphaltene (pitch) M14 A by solvent deasphalting, and a hydrodemetalizating/desulfurizing process 22 A wherein a mixture of the deasphalted oil M13 A and the vacuum gas oil M11 A is subjected to hydrodemetalizating/desulfurizing process thereby to produce HDMS refined oil M15 A.
  • a vacuum fractional distillation process 20 A wherein the residue M2A is separated into vacuum gas oil M11 A and vacuum residue M12 A by vacuum distillation
  • a solvent deasphalting process 21 A wherein the vacuum residue M12 A is separated into deasphalted oil M13
  • the residue M2A is introduced into a vacuum distillation tower where the M2A is distilled and separated into a low-boiling point component and a high-boiling point component, while the vacuum gas oil M11 A having the lower boiling point is obtained from the top of the tower and the vacuum residue M12 A having the higher boiling point is obtained from the bottom of the tower.
  • the vacuum fractional distillation process 20 A is followed by the solvent deasphalting process 21 A where the vacuum residue M12 A obtained in the former process is separated into deasphalted oil M13 A and asphaltene (pitch) M14 A. While the vacuum fractional distillation process is similar to the cases shown in FIG. 4 and FIG. 5, the extraction ratio of the deasphalted oil M13 A obtained in the solvent deasphalting process of the vacuum residue is controlled so that the desirable upper limit of the vanadium (V) content rises to, for example, 70 wt ppm in correspondence to the concentrations of metals, residual carbon, and sulfur in M13 A that are higher than those of the residue M2A.
  • V vanadium
  • the demetalizing and desulfurizing conditions for the HDMS refined oil M1SA thus obtained are preferably selected so as to achieve the vanadium (V) content of 2 wt ppm or lower, preferably 1 wt ppm or lower, and a sulfur content of 0.5 wt % or lower, preferably 0.3 wt % or lower.
  • the remainder of the HDMS refined oil M15 obtained in the hydrodemetalizating/desulfurizing process 22 A that is not fed to the sixth mixing process 23 A may be used as an intermediate oil product to be used as the feed for the fluid catalytic cracking (FCC) process or the feed for the hydrocracking (HCR) process.
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • the M13 A and M11 A may be, instead of being mixed, subjected to hydrodemetalizating/desulfurizing process in separate reactors each under optimum conditions, and then mixed with each other, or at least part of the vacuum gas oil M11 A that has been subjected to the hydrodemetalizating/desulfurizing process and at least a part of the distillate M3 A are mixed thereby to obtain gas turbine fuel (GTF) that has vanadium (V) content of 0.5 wt ppm or lower.
  • GTF gas turbine fuel
  • V vanadium
  • the vanadium (V) content of the mixed oil becomes sufficiently low and it is possible to obtain gas turbine fuel as one of the petroleum products. It is also possible to produce intermediate oil products of low metal content (V+Ni) used as the feed for a fluid catalytic cracking or a hydrocracking process even from the remainder of the HDMS refined oil M15 A obtained from a mixture of the vacuum gas oil M7A and the deasphalted oil M13 A by hydrodemetalizating/desulfurizing process. Thus a plurality of intermediate oil products having a high added value can be produced efficiently.
  • the yield of deasphalted oil M13 A in the solvent deasphalting process 21 A can be improved by producing the gas turbine fuel (GTF) and feed for the fluid catalytic cracking (FCC) process or feed for the hydrocracking (HCR) process at the same time, thereby suppressing the production of asphaltene (pitch) M14 A from the vacuum residue M12 A.
  • GTF gas turbine fuel
  • FCC fluid catalytic cracking
  • HCR hydrocracking
  • a plurality of oil products including gas turbine fuel and intermediate oil products to be used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 7 by the oil refining method shown in FIG. 1.
  • distillate M1 thus obtained was desulfurized in hydrorefining process 2 in the presence of hydrogen and catalyst, thereby to obtain hydrorefined oils M3, M3 ′.
  • M3 ′ was used as a petroleum product, naphtha, without applying further processing.
  • the yield of the hydrorefined oil M3 was 13.0 wt % of the feed oil and the sulfur content was 0.02 wt %.
  • the yield of naphtha M3 ′ was 2 wt % of the feed oil.
  • the residue M2 was subjected to the solvent deasphalting process 3 in a solvent extraction tower using isobutane as the solvent, thereby to obtain deasphalted oil M4 with 65% extraction ratio and asphaltene (pitch) M5 as the residue.
  • the ratio of the solvent to the residue M2 (solvent/M2) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M4 was 54.3 wt % of the feed oil, while the sulfur content was 3.60 wt %, the vanadium content was 66 wt ppm, and the extraction ratio was 14%.
  • the yield of the asphaltene (pitch) M5 was 29.2 wt % of the feed oil.
  • the deasphalted oil M4 thus obtained was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 3:7 in volume proportion, thereby to obtain the HDMS refined oil M6 through hydrodemetalizating/desulfurizing process 4 in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 100 atm, and the H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.7/hr and the reaction temperature was 370° C.
  • the yield of the HDMS refined oil M6 was 51 wt % of the feed oil, the sulfur content was 0.4 wt %, and the vanadium content was 0.7 wt ppm.
  • a plurality of oil products including gas turbine fuel and intermediate oil products to be used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 8 by the oil refining method shown in FIG. 2.
  • the ultra heavy crude (Orinoco oil) having an API gravity of 8.5, a sulfur content of 3.67 wt % and a vanadium content of 393 wt ppm was used as feed oil that was first distilled under atmospheric pressure (fractional distillation process 1 ) in a topper thereby to obtain distillate M1 and residue M2.
  • the yield of the distillate M1 was 15.9 wt % of the feed oil and the sulfur content was 2.41 wt %.
  • the yield of the residue M2 was 83.5 wt % of the feed oil, while the sulfur content was 4.07 wt % and the vanadium content was 472 wt ppm.
  • distillate M1 thus obtained was desulfurized in hydrorefining process 2 in the presence of hydrogen and catalyst, thereby to obtain hydrorefined oils M3, M3 ′.
  • M3 ′ was used as a petroleum product, naphtha, without applying further processing.
  • the yield of the hydrorefined oil M3 was 13.0 wt % of the feed oil and the sulfur content was 0.02 wt %.
  • the yield of naphtha M3 ′ was 2 wt % of the feed oil.
  • the residue M2 was subjected to the solvent deasphalting process 3 in a solvent extraction tower using pentane as the solvent, thereby to obtain deasphalted oil M4 with a 76.6% extraction ratio and asphaltene (pitch) M5 as the residue.
  • the ratio of the solvent to the residue M2 (solvent/M2) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M4 was 64 wt % of the feed oil, the sulfur content was 3.9 wt %, the vanadium content was 130 wt ppm and the extraction ratio was 27.5%.
  • the yield of the asphaltene (pitch) M5 was 19.5 wt % of the feed oil.
  • the deasphalted oil M4 thus obtained was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 5:5 in volume proportion, thereby to obtain the HDMS refined oil M6 through hydrodemetalizating/desulfurizing process 4 in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 100 atm, H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.5/hr and reaction temperature was 370° C.
  • the yield of the HDMS refined oil M6 was 59 wt % of the feed oil, the sulfur content was 0.45 wt %, and the vanadium content was 8 wt ppm.
  • the HDMS refined oil M6 thus obtained was distilled in a vacuum (vacuum fractional distillation process 6 ) thereby to obtain a vacuum gas oil (VGO) M7 and the vacuum residue M8.
  • VGO vacuum gas oil
  • the yield of the vacuum gas oil M7 was 25 wt % of the feed oil, the sulfur content was 0.24 wt %, and the vanadium content was 0.3 wt ppm.
  • All of the vacuum gas oil M7 was mixed with the hydrorefined oil M3 (second mixing process 7 ) thereby to produce gas turbine fuel (GTF) with a yield of 38 wt % of the feed oil, a sulfur content of 0.16 wt %, and a vanadium content of 0.19 wt ppm.
  • GTF gas turbine fuel
  • the vacuum residue M8 obtained in the vacuum fractional distillation process was used as a feed stock for the fluid catalyst cracking (FCC) process or a feed stock for the hydrocracking (HCR) process without applying further processing.
  • the feed stock for the fluid catalyst cracking (FCC) process or the feed stock for the hydrocracking (HCR) process may also be obtained by mixing a part of the deasphalted oil M4 or a part of the HDMS refined oil M6 with the vacuum residue M8.
  • the feed stock for the fluid catalyst cracking (FCC) process or the feed stock for the hydrocracking (HCR) process that is obtained in this way showed yield of 34 wt % of the feed oil, a sulfur content of 0.60 wt %, and a vanadium content of 13.7 wt ppm.
  • a plurality of oil products including gas turbine fuel and intermediate oil products to be used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 9 by the oil refining method shown in FIG. 3.
  • the residue M2 thus obtained was subjected to vacuum fractional distillation process 20 thereby to obtain a vacuum gas oil M11 and vacuum residue M12 .
  • the yield of the vacuum gas oil M11 was 28.2 wt % of the feed oil, the sulfur content was 3.37 wt %, and the vanadium content was 1.5 wt ppm.
  • the yield of the vacuum residue M12 was 30.6 wt % of the feed oil, the vanadium content was 223 wt ppm, (V+Ni) content was 294 wt ppm, residual carbon content was 24.4% and the sulfur content was 6.04 wt %.
  • the vacuum residue M12 was subjected to the solvent deasphalting process 21 in a solvent extraction tower using isobutane as the solvent, thereby to obtain deasphalted oil M13 with a 60% extraction ratio and asphaltene (pitch) M14 as the residue.
  • the ratio of the solvent to the vacuum residue M12 (solvent/M12 ) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M13 was 18.4 wt % of the feed oil, the sulfur content was 4.62 wt %, the vanadium content was 22 wt ppm and the extraction ratio was 19%.
  • the yield of the asphaltene (pitch) M14 was 12.2 wt % of the feed oil.
  • a mixture of the deasphalted oil M13 and the vacuum gas oil M11 was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 1:9 in volume proportion, thereby to obtain the HDMS refined oil M15 through hydrodemetalizating/desulfurizing process 4 in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 90 atm, the H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.7/hr and reaction temperature was 370° C.
  • the yield of the HDMS refined oil M15 was 44 wt % of the feed oil, the sulfur content was 0.6 wt %, and the vanadium content was 1.0 wt ppm.
  • a plurality of oil products including gas turbine fuel and intermediate oil products to be used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 10 by the oil refining method shown in FIG. 4.
  • a low-sulfur content crude oil (Arabian light) having a sulfur content of 1.79 wt % and a vanadium content of 13.5 wt ppm was used as feed oil that was first distilled under atmospheric pressure (fractional distillation process 1 A) in a topper thereby to obtain distillate M1A and residue M2A.
  • the yield of the distillate M1A was 53.5 wt % of the feed oil and the sulfur content was 0.63 wt %.
  • the yield of the residue M2A was 45.4 wt % of the feed oil, while the sulfur content was 3.20 wt % and the vanadium content was 30.0 wt ppm.
  • distillate M1A thus obtained was separated in a flasher 30 thereby to obtain distillates M3 A, M3 A′.
  • M3 ′ was used as a petroleum product, naphtha, without applying further processing.
  • the yield of the distillate M3 A was 50.9 wt % of the feed oil and the sulfur content was 0.66 wt %.
  • the yield of naphtha M3 ′ was 2.6 wt % of the feed oil.
  • the residue M2A was subjected to the solvent deasphalting process 3 A in a solvent extraction tower using isobutane as the solvent, thereby to obtain deasphalted oil M4A with 65% extraction ratio and asphaltene (pitch) M5A as the residue.
  • the ratio of the solvent to the residue M2A (solvent/M2A) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M4A was 38.6 wt % of the feed oil, the sulfur content was 2.80 wt %, and the vanadium content was 5.9 wt ppm.
  • the yield of the asphaltene (pitch) M5A was 6.8 wt % of the feed oil.
  • the deasphalted oil M4A thus obtained was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 1:9 in volume proportion, thereby to obtain the HDMS refined oil M6A through hydrodemetalizating/desulfurizing process 4 A in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 100 atm, H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.5/hr and the reaction temperature was 370° C.
  • the yield of the HDMS refined oil M6A was 36.3 wt % of the feed oil, the sulfur content was 0.10 wt %, and the vanadium content was 0.9 wt ppm.
  • a plurality of oil products including gas turbine fuel and intermediate oil products to be used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 11 by the oil refining method shown in FIG. 5.
  • the low-sulfur content crude oil (Arabian light), the same oil as that used in the fourth experimental example, having a sulfur content of 1.79 wt % and a vanadium content of 13.5 wt ppm was used as the feed oil that was first distilled under atmospheric pressure (fractional distillation process 1 A) in a topper thereby to obtain distillate M1A and residue M2A.
  • the yield of the distillate M1A was 53.5 wt % of the feed oil and the sulfur content was 0.63 wt %.
  • the yield of the residue M2A was 45.4 wt % of the feed oil, while the sulfur content was 3.20 wt % and the vanadium content was 30.0 wt ppm.
  • the distillate M1A thus obtained was separated in the flasher 30 thereby to obtain distillates M3 A, M3 A′.
  • the distillate M3 A was used as a petroleum product, naphtha, without applying further processing.
  • the yield of the distillate M3 A was 50.9 wt % of the feed oil and the sulfur content was 0.66 wt %.
  • the yield of naphtha M3 A′ was 2.6 wt % of the feed oil.
  • the residue M2A was subjected to the solvent deasphalting process 3 A in a solvent extraction tower using pentane as the solvent, thereby to obtain deasphalted oil M4A with 65% extraction ratio and asphaltene (pitch) M5A as the residue.
  • the ratio of the solvent to the residue M2A (solvent/M2) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M4A thus obtained was 38.6 wt % of the feed oil, the sulfur content was 2.80 wt %, and the vanadium content was 5.9 wt ppm.
  • the yield of the asphaltene (pitch) M5A was 6.8 wt % of the feed oil.
  • the deasphalted oil M4A was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 1:9 in volume proportion, thereby to obtain the HDMS refined oil M6A through hydrodemetalizating/desulfurizing process 4 A in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 100 atm, H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.7/hr and the reaction temperature was 360° C.
  • the yield of the HDMS refined oil M6A was 36.3 wt % of the feed oil, the sulfur content was 0.30 wt %, and the vanadium content was 1.5 wt ppm.
  • the HDMS refined oil M6A thus obtained was distilled in a vacuum (vacuum fractional distillation process 6 A) thereby to obtain a vacuum gas oil (VGO) M7A and the vacuum residue M8A.
  • VGO vacuum gas oil
  • the yield of the vacuum gas oil M7A thus obtained was 23.0 wt % of the feed oil, the sulfur content was 0.10 wt %, and the vanadium content was 0.2 wt ppm.
  • All of the vacuum gas oil M7A was mixed with the distillate M3 A (fifth mixing process 7 A) thereby to produce gas turbine fuel (GTF) that included a sulfur content of 0.49 wt % and a vanadium content of 0.06 wt ppm, with a yield of 73.9 wt % of the feed oil.
  • GTF gas turbine fuel
  • the vacuum residue M8A obtained in the vacuum fractional distillation process was used as a feed stock for the fluid catalyst cracking (FCC) process or a feed stock for the hydrocracking (HCR) process without applying further processing.
  • the feed stock for the fluid catalyst cracking (FCC) process or the feed stock for the hydrocracking (HCR) process may also be obtained by mixing a part of the deasphalted oil M4A or a part of the HDMS refined oil M6A with the vacuum residue M8A.
  • the feed stock for the fluid catalyst cracking (FCC) process or the feed stock for the hydrocracking (HCR) process obtained in this way showed yield of 13.3 wt % of the feed oil, a sulfur content of 0.65 wt %, and a vanadium content of 3.7 wt ppm.
  • a plurality of oil products including gas turbine fuel and intermediate oil products used as the feed for a fluid catalytic cracking or a hydrocracking process were produced as shown in FIG. 12 by the oil refining method shown in FIG. 6.
  • the low-sulfur content crude oil (Arabian light), the same oil as that used in the fourth experimental example, having a sulfur content of 1.79 wt % and a vanadium content of 13.5 wt ppm was used as feed oil that was first distilled under atmospheric pressure (fractional distillation process 1 A) in a topper thereby to obtain distillate M1A and residue M2A.
  • the yield of the distillate M1A was 53.5 wt % of the feed oil and the sulfur content was 0.63 wt %.
  • the yield of the residue M2A was 45.4 wt % of the feed oil, while the sulfur content was 3.20 wt % and the vanadium content was 30.0 wt ppm.
  • the residue M2A thus obtained was distilled in a vacuum (vacuum fractional distillation process 20 A) thereby to obtain a vacuum gas oil M11 A and vacuum residue M12 A.
  • the yield of the vacuum gas oil M11 A was 30.4 wt % of the feed oil, while the sulfur content was 2.70 wt % and the vanadium content was 0.1 wt ppm.
  • the yield of the vacuum residue M12 A was 15.0 wt % of the feed oil, while the vanadium content was 91.0 wt ppm and the sulfur content was 4.10 wt %.
  • the distillate M1A was separated in the flasher 30 thereby to obtain distillates M3 A, M3 A′.
  • the distillate M3 A′ was used as one of the petroleum product, naphtha, without applying further processing.
  • the yield of the distillate M3 A was 50.9 wt % of the feed oil and the sulfur content was 0.66 wt %.
  • the yield of naphtha M3 A′ was 2.6 wt % of the feed oil.
  • the vacuum residue M12 A was subjected to the solvent deasphalting process 21 A in a solvent extraction tower using isobutane as the solvent, thereby to obtain deasphalted oil M13 A with a 60% extraction ratio and asphaltene (pitch) M14 A as the residue.
  • the ratio of the solvent to the vacuum residue M12 A (solvent/M12 A) in the solvent deasphalting process was set to 8.
  • the yield of the deasphalted oil M13 A was 10.5 wt % of the feed oil, the sulfur content was 3.30 wt %, and the vanadium content was 11.0 wt ppm.
  • the yield of the asphaltene (pitch) M14 A was 4.5 wt % of the feed oil.
  • a mixture of the deasphalted oil M13 A and the vacuum gas oil M11 A was introduced into a reactor filled with a hydrodemetalizing catalyst and a hydrodesulfurizing catalyst in a ratio of 1:9 in volume proportion, thereby to obtain the HDMS refined oil M15 A through hydrodemetalizating/desulfurizing process 22 A in the presence of hydrogen and the catalysts.
  • the process conditions were set to partial pressure of hydrogen of 100 atm, H 2 to oil ratio of 800 Nl/l.
  • the LHSV was 0.5/hr and the reaction temperature was 375° C.
  • the yield of the HDMS refined oil M15 A was 38.4 wt % of the feed oil, while the sulfur content was 0.10 wt %, and the vanadium content was 0.9 wt ppm.
  • the oil refining method according to the present invention makes it possible to produce, for example, oil product (gas turbine fuel) having vanadium (V) content of 0.5 wt ppm or lower, and intermediate oil products having metal (V+Ni) content of 30 wt ppm or lower that is suitable as the feed stock to be used in the fluid catalyst cracking (FCC) process or in the hydrocracking (HCR) process, from a heavy feed oil such as Orinoco tar or a feed oil having low sulfur content.
  • oil product gas turbine fuel
  • V+Ni vanadium
  • HCR hydrocracking

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US20080223751A1 (en) * 2005-09-21 2008-09-18 Eric Lenglet Non Asphaltenic Oil
US20090036267A1 (en) * 2007-08-02 2009-02-05 Bellinger Steven M System and Method for Controlling Transmission Shift Points Based on Vehicle Weight
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US20110094937A1 (en) * 2009-10-27 2011-04-28 Kellogg Brown & Root Llc Residuum Oil Supercritical Extraction Process
US20110142729A1 (en) * 2009-12-11 2011-06-16 Uop Llc Apparatus for producing hydrocarbon fuel
US20110139681A1 (en) * 2009-12-11 2011-06-16 Uop Llc Process for producing hydrocarbon fuel
US20110139676A1 (en) * 2009-12-11 2011-06-16 Uop Llc Composition of hydrocarbon fuel
WO2011071705A3 (en) * 2009-12-11 2011-10-20 Uop Llc Process and apparatus for producing hydrocarbon fuel and composition
US8728300B2 (en) 2010-10-15 2014-05-20 Kellogg Brown & Root Llc Flash processing a solvent deasphalting feed
WO2014096602A1 (fr) 2012-12-18 2014-06-26 IFP Energies Nouvelles Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif
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AU2002222568B2 (en) 2006-08-31
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RU2270230C2 (ru) 2006-02-20
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KR20030053062A (ko) 2003-06-27
CN100387690C (zh) 2008-05-14

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