EP2256179B1 - Verfahren zur Herstellung einer Kohlewasserstofffraktion mit hohem Oktan- und niedrigem Schwefelgehalt - Google Patents

Verfahren zur Herstellung einer Kohlewasserstofffraktion mit hohem Oktan- und niedrigem Schwefelgehalt Download PDF

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Publication number
EP2256179B1
EP2256179B1 EP10290246.7A EP10290246A EP2256179B1 EP 2256179 B1 EP2256179 B1 EP 2256179B1 EP 10290246 A EP10290246 A EP 10290246A EP 2256179 B1 EP2256179 B1 EP 2256179B1
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sent
gasoline
stage
raffinate
process according
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French (fr)
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EP2256179A2 (de
EP2256179A3 (de
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Quentin Debuisschert
Jacinthe Frécon
Robert L. Huggins
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
    • 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
    • C10G35/00—Reforming naphtha
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • 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
    • C10G2300/1096—Aromatics or polyaromatics
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel

Definitions

  • the present invention relates to the field of improving the octane number of a hydrocarbon fraction, and more particularly to a process for producing a high octane and low sulfur hydrocarbon fraction, which makes it possible to value the entire cut, reduce the total sulfur content of the cut to very low levels, while increasing the octane number of the cut.
  • Petroleum refining and petrochemicals are now subject to new constraints. Indeed, all countries are gradually adopting strict specifications of sulfur, the goal is to reach between 5 to 10 ppm of sulfur.
  • the problem of reduction of sulfur contents is essentially concentrated on the species obtained by cracking, whether catalytic (FCC Fluid Catalytic Cracking according to the English terminology) or non-catalytic (coking, visbreaking, steam cracking), main sulfur precursors. in the gasoline pools.
  • a second constraint comes from the fact that the fuel market shows a steady decline in the demand for gasoline in favor of diesel while maintaining a high demand of gasoline quality in terms of octane, vapor pressure Reid and sulfur content. It is therefore important to produce gasoline of improved quality but in reduced quantity for the benefit of distillates (kerosene and diesel).
  • a third constraint comes from the petrochemical industry and in particular the steam cracking and catalytic reforming processes which produce the highest value of olefins and aromatics (ethylene and propylene) respectively, and the price of its raw materials (especially naphthas). alarmingly, and this in the long term because of future resource constraints and which require low aromatic loads.
  • the patent EP1370627 discloses a process for producing low sulfur gasoline comprising at least one selective hydrogenation of the diolefins present in the initial gasoline, a step of transforming the light sulfur compounds present in the gasoline, a fractionation of the gasoline obtained in at least two fractions, a light fraction and a heavy fraction, and a desulfurization treatment in one step of at least a portion of the heavy fraction resulting from the fractionation.
  • This process thus makes it possible to reduce the amount of sulfur present in gasoline and to obtain gasolines whose octane number is better than that which could be obtained simply by hydrotreatment. However, even if the octane number is improved, compared to that obtained with a hydrotreatment, it is ultimately degraded, ie less than that of the treated feedstock.
  • the patent US 3044950 discloses a process for upgrading an essence of FCC to the gasoline pool which comprises a step of distilling said gasoline into two or three slices and a hydrotreating step (HDS and total hydrogenation of olefins) of the heaviest cut resulting from distillation. Finally, the heavy desulfurized cut is subjected to a step of extraction of the aromatic compounds from which is recovered an aromatic enriched extract and a paraffin-rich raffinate. According to the patent US 3044950 , the paraffinic raffinate is fully processed in a catalytic reforming unit to produce a rich aromatic effluent that is sent to the gasoline pool.
  • the present invention provides a process for producing a hydrocarbon fraction with a high octane number and a low sulfur content from a hydrocarbon feedstock, according to claim 1.
  • the hydrocarbon feedstock is derived from a catalytic cracking unit or a thermal cracking unit or a coker unit or a visbreaking unit.
  • the hydrodesulfurization step is selective and carried out in one step in one or two reactors or in two stages.
  • the hydrodesulfurization step is non-selective.
  • At least a portion of the paraffinic raffinate is sent to a separation step which leads to a light raffinate sent to the gasoline pool, in admixture with the aromatic extract, and / or to a unit steam cracking or a catalytic reforming unit and a heavy raffinate sent to the diesel pool or to the kerosene pool.
  • the light hydrocarbon fraction is sent in admixture with the aromatic extract and a part of the paraffinic raffinate to the gasoline pool.
  • the aromatic extraction step is a liquid-liquid extraction or an extractive distillation.
  • the step of extracting the aromatic compounds is a liquid-liquid extraction with a solvent level of between 1.5 and 5.
  • the process illustrated on figures 1 , 2 and 3 consists in producing a hydrocarbon fraction with high octane number and low sulfur content.
  • the filler used in the process according to the invention is a sulfur-containing hydrocarbon feedstock whose boiling point extends from the boiling point of the hydrocarbon feeds containing 4 carbon atoms (C 4 ) up to the point of boiling point. 300 ° C final boiling according to ASTM D86.
  • the hydrocarbon feedstock used in the process according to the invention may be, for example, a petrol cut from a catalytic cracking unit, a thermal cracking unit (Steam Cracker), a coker unit (coker according to the English terminology) or a visbreaking unit (visbreaker according to the English terminology).
  • the hydrocarbon feedstock is subjected to at least one hydrodesulfurization treatment and an extraction treatment of the aromatic compounds.
  • the charge is sent via line (1) to a hydrodesulfurization unit (C).
  • the effluent from the hydrodesulfurization unit (C) flows via line (4) before being sent to the aromatics extraction unit (D).
  • the aromatic extract also called extract enriched in aromatics by contribution to the charge
  • the paraffinic raffinate also called paraffin enriched raffinate with respect to the feedstock
  • the paraffinic raffinate also called paraffin enriched raffinate with respect to the feedstock
  • Part of this paraffinic raffinate is sent via line (7) to a steam cracking unit.
  • paraffinic raffinate The other part of this paraffinic raffinate is sent via line (8) to the gasoline pool.
  • the sequencing of the hydrodesulphurization and extraction stages of the aromatic compounds makes it possible to valorise the totality of a hydrocarbon feedstock and in particular of a gasoline cut by reducing the sulfur content and maximizing the octane number of the feedstock.
  • Part of the gasoline can be converted into medium distillate with low sulfur content.
  • Another part of the gasoline can be used as a petrochemical base by being sent to a steam cracking unit.
  • the process thus makes it possible to meet the abovementioned constraints by reducing the quantity of gasoline produced from a hydrocarbon feedstock in favor of a better raffinate for petrochemicals.
  • a selective hydrogenation unit A
  • the effluent from the selective hydrogenation unit (A) flows via the line (2) and is then injected into a separation column (B) which leads to at least two cuts: a light gasoline cut sent to the gasoline pool via line (5); this light cut will have a maximum ASTM D86 end point of 160 ° C, preferably 120 ° C and very preferably 90 ° C, a heavy gasoline cut flowing via the line (3) and possibly an intermediate gasoline cut flowing via the line (18).
  • This intermediate slice generally has an ASTM D86 boiling point of less than or equal to 220 ° C, preferably less than or equal to 180 ° C and very preferably less than or equal to 160 ° C.
  • an intermediate cut (18) is produced, it is sent to the hydrodesulfurization unit (C) via the line (18).
  • the heavy cut flowing via the line (3) is sent to the middle distillates after hydrotreatment if necessary. In the case where there is no intermediate cut, it is the heavy cut that is sent to the hydrodesulfurization unit (C) via the line (3).
  • the effluent from the hydrodesulfurization unit (C) flows via line (4) before being sent to the aromatics extraction unit (D).
  • the paraffinic raffinate circulates via line (6). Part of this paraffinic raffinate is sent via line (7) to a steam cracking unit. The other part of this paraffinic raffinate is sent via line (8) to the gasoline pool.
  • the effluents (light gasoline and aromatic extract) circulating in the lines (9) and (5), are mixed via the line (11), before being sent in mixture with the effluent (paraffinic raffinate) circulating via the line ( 8) to the gasoline pool.
  • This variant of the process according to the invention makes it possible, at the moment of the separation step, to obtain a cut of light petrol containing less than 10 ppm of sulfur and a cut of heavy gasoline with a controlled olefin content, which implies a 15 to 85% decrease in olefins sent to the hydrodesulfurization unit.
  • the aromatics extraction step may be followed by a separation step.
  • the feed is sent via line (1) to the selective hydrogenation unit (A).
  • the effluent from the selective hydrogenation unit (A) flows via the line (2) and is then injected into a separation column (B) which leads to two cuts: a gasoline cut lightly sent to the gasoline pool via line 5 and a heavy gasoline cut sent to the hydrodesulfurization unit (C) via line (3).
  • the effluent from the hydrodesulfurization unit (C) flows via line (4) before being sent to the aromatics extraction unit (D).
  • the paraffinic raffinate circulates via line (6).
  • the effluents (light gasoline and aromatic extract) circulating in lines (9) and (5) are mixed via line (11).
  • the paraffinic raffinate circulating via the line (6) is sent to a separation column (E).
  • the heavy raffinate is sent to the diesel cut via line (13).
  • the light raffinate flows via line (14). Part of this light raffinate is sent via line (15) to the gasoline pool and the other part is sent via line (16) to the steam cracker.
  • the effluent circulating via the line (11) is mixed with the effluent circulating via the line (15) to give the effluent circulating via the line (17) which is sent to the gasoline pool.
  • This variant can be used in the case where it is desirable to maximize the production of distillates, without sending product to the petrochemical industry.
  • the hydrocarbon feedstock without any selective hydrogenation step or separation, is subjected to at least one hydrodesulfurization treatment and an extraction treatment of the aromatic compounds which can be followed by a step of seperation.
  • the charge is sent to a hydrodesulfurization unit.
  • the effluent from the hydrodesulfurization unit is sent to the aromatics extraction unit.
  • the paraffinic raffinate obtained at the outlet of the aromatics extraction unit is sent to a separation column.
  • the heavy raffinate is sent to the diesel cutter.
  • Some of the light raffinate is sent to the gasoline pool and the other part is sent to the steam cracker.
  • the aromatic extract from the extraction unit is mixed with the other part of the light raffinate, and then sent to the gasoline pool.
  • the process according to the invention comprises a step of selective hydrogenation. This step is intended to convert the diolefins, present in the hydrocarbon feedstock, into olefins. During this stage it is also possible to weigh down the light sulfur products present in the hydrocarbon feedstock.
  • This selective hydrogenation step takes place in a reactor generally in the presence of a catalyst containing at least one Group VIII metal, preferably selected from the group formed by platinum, palladium and nickel, and a support. It is possible, for example, to use a catalyst based on nickel or palladium deposited on an inert support, such as, for example, alumina, silica or a support containing at least 50% of alumina.
  • a catalyst based on nickel or palladium deposited on an inert support such as, for example, alumina, silica or a support containing at least 50% of alumina.
  • Another metal may be associated with the main metal to form a bimetallic catalyst, such as, for example, molybdenum or tungsten.
  • a bimetallic catalyst such as, for example, molybdenum or tungsten.
  • the step is carried out under pressure and in the presence of a quantity of hydrogen in small excess relative to the stoichiometric value necessary to hydrogenate the diolefins.
  • the hydrogen and the feedstock to be treated are injected in ascending or descending streams into a reactor generally comprising a fixed bed of catalyst.
  • the pressure employed during the selective hydrogenation reaction must be sufficient to maintain more than 60% by weight of the batch to be treated in the liquid phase in the reactor, preferably more than 80%, and more preferably more than 95% .
  • the pressure is thus generally between, for example, 0.4 and 5 MPa, preferably greater than 1 MPa, and more preferably between 1 and 4 MPa.
  • the hourly space velocity of the charge to be treated is between about 1 and about 20 h -1 (volume of charge per volume of catalyst per hour), preferably between 2 and 10 h -1 , very preferably between 2 and 10 h -1. 8 h -1 .
  • the temperature is most generally between about 50 ° C and about 250 ° C, and preferably between 80 ° C and 220 ° C, and more preferably between 100 ° C and 200 ° C, to ensure a sufficient conversion of diolefins.
  • the ratio of hydrogen on charge expressed in liters is generally between 3 and 50 liters per liter, preferably between 3 and 20 liters per liter.
  • the diolefin content is generally reduced to less than 3000 ppm, and preferably less than 1500 ppm.
  • this hydrogenation step can be carried out by passing, for example, the initial carbonaceous feedstock over a catalyst capable of both hydrogenating the diolefins and converting the light sulfur compounds or the olefins into heavier sulfur compounds, or on a separate catalyst (same or different) but to achieve this transformation in the same reactor as the hydrogenation step.
  • This separation step is preferably carried out by means of a conventional distillation / fractionation column.
  • This fractionation column must make it possible to separate at least the light fraction of the feedstock resulting from the hydrogenation containing a small fraction of sulfur and the heavy fraction containing most of the sulfur initially present in the initial charge.
  • This column generally operates at a pressure of between 0.1 and 2 MPa and preferably between 0.1 and 1 MPa.
  • the number of theoretical plates of this separation column is generally between 10 and 100 and preferably between 20 and 60.
  • the reflux ratio expressed as the ratio of the liquid traffic in the column divided by the distillate flow rate expressed in kg / h, is generally between 0.1 and 2, preferably greater than 0.5.
  • the light gasoline obtained after the separation generally contains at least 50% of C 5 olefins, and preferably at least 90%, optionally of C5 compounds, C6 olefins and C 7 compounds.
  • this light fraction has a low sulfur content, ie it is not generally necessary to treat the light cut before using it as fuel.
  • the process according to the invention comprises a hydrodesulfurization step. This step can be carried out either directly on the initial charge or on the heavy cut obtained at the end of the separation step.
  • the hydrodesulfurization carried out as part of the process may be selective (with a controlled olefin saturation rate, that is to say the conservation of a portion of the olefins) or non-selective (saturation of the olefins).
  • This step is generally carried out in at least one reactor in the presence of a catalyst comprising at least one element of group VIII.
  • Selective hydrodesulfurization can be carried out either in one step or in two steps.
  • the catalyst and process conditions used in the reactor 1 are similar to that described in the case of a single reactor
  • the catalysts used are generally catalysts comprising cobalt and molybdenum or catalysts comprising nickel.
  • the temperature in the 2 nd reactor is generally between 250 and 400 ° C and preferably between 300 and 370 ° C.
  • the space velocity of the liquid is for example between 0.5 and about 10 h -1 (expressed in volume of liquid per volume of catalyst per hour), and preferably between 1 and 8 h -1 .
  • the conditions of pressure and H 2 / HC are similar to those of the reactor 1 to the 1 st step.
  • This configuration (and in particular the decoupling of temperatures and the use of catalyst sequencing) makes it possible to be more selective than in the configuration with a single reactor.
  • the preservation of olefins through the HDS stage is therefore better.
  • the catalyst used is generally a catalyst comprising cobalt and molybdenum in the two steps.
  • This configuration makes it possible to be even more selective thanks to the intermediate elimination of H 2 S between the two stages, which reduces the partial pressure of H 2 S.
  • the conversion of the olefins by hydrogenation observed is from 5 to 95%, preferably from 15 to 85%, and very preferably from 15 to 50%.
  • This step is carried out in the presence of hydrogen, at a temperature for example between 200 ° C and 400 ° C, preferably between 220 ° C and 350 ° C under a pressure generally between 0.5 and 5 MPa, preferably between 1 and 3 MPa, and very preferably between 1.5 and 3 MPa.
  • the space velocity of the liquid is for example between 0.5 and about 10 h -1 (expressed in volume of liquid per volume of catalyst per hour), and preferably between 1 and 8 h -1 .
  • the H 2 / HC ratio is adjusted according to the desired hydrodesulphurization rates in the range of, for example, between 100 and 600 liters per liter, and preferably between 100 and 350 liters per liter.
  • the catalyst used is generally a catalyst comprising cobalt and molybdenum or nickel and molybdenum.
  • the catalysts used have a higher hydrogenating activity than in the case of a selective hydrodesulfurization
  • the conversion of unsaturated sulfur compounds is greater than 15% and preferably greater than 90%.
  • the reduction in olefins observed is greater than 50%, preferably greater than 85%, and very preferably greater than 95%.
  • the process according to the invention comprises a step of extracting the aromatic compounds.
  • This extraction is either a liquid-liquid extraction or an extractive distillation using one or more solvents.
  • the extraction is carried out using any type of solvent well known to those skilled in the art to carry out such extractions and for example solvents of sulfolane type, dimethylsulfoxide. (DMSO), dimethylformamide (DMF), N-methylpyrrolidone (NMP), N-formylmorpholine (NFM), methanol, acetonitrile and mixtures of these various solvents.
  • DMSO dimethylformamide
  • NMP N-methylpyrrolidone
  • NMF N-formylmorpholine
  • methanol acetonitrile and mixtures of these various solvents.
  • the effluent obtained after the hydrodesulfurization step is contacted with the solvent in a first extraction column from which are recovered a solvent rich in aromatic compounds, and a raffinate consisting of non-aromatic compounds.
  • the raffinate is subsequently purified in a washing column to remove residual traces of solvent.
  • the solvent rich in aromatic compounds is conventionally first freed of the last nonar
  • a non-volatile and miscible high-boiling separation solvent is used to modify the relative volatility (vapor pressure) of the constituents of a mixture whose volatility is very close.
  • the solvent interacts differently with the different components of the mixture, thus causing a difference in the relative volatility of each component and making it possible to separate them.
  • the technique involves sending the stream comprising the aromatic compounds with a solvent into an extractive distillation column.
  • the non-aromatic compounds are removed from the top of the column with a small amount of solvent (which is then regenerated).
  • the aromatic compounds are removed from the bottom of the column with the solvent.
  • the solvent / aromatic compounds group is sent to a separation column or the purified aromatic compounds are separated from the solvent.
  • the solvent employed is well known to those skilled in the art such as N-formylmorpholine.
  • the aromatic extract obtained makes it possible to remove the low octane molecules present in the feedstock and thus generally contributes to exceeding the required specifications of Octane Research Index (or RON for Research Octane Number, according to the English thermology Saxon) of 95 and Octane Engine Index (or MON for Motor Octane Number according to English terminology) 85 of the gasoline pool after remixing with other typical constituents (reformate, isomerate, ethers, ).
  • the paraffinic raffinate obtained generally constitutes an excellent feedstock for a steam cracking or catalytic reforming unit and thus replaces the very expensive naphtha.
  • the process according to the invention may comprise a step of separating the raffinate, obtained at the step of extracting the aromatic compounds, in at least two cuts, a light cut that can be sent to the gasoline pool or to the petrochemical and a cut. heavy that can be sent to the kerosene or diesel pool.
  • This separation is preferably carried out by means of a conventional distillation column.
  • This column generally operates at a pressure of between 0.01 and 2 MPa and preferably between 0.01 and 0.5 MPa.
  • the number of theoretical plates of this separation column is generally between 10 and 100 and preferably between 20 and 60.
  • the reflux ratio expressed as the ratio of the liquid traffic in the column divided by the distillate flow expressed in kg / h, is generally greater than 0.2 and preferably greater than 0.4
  • HR 806 type Cobalt / Molybdenum catalyst
  • the effluent obtained in the hydrodesulfurization stage is sent via line (4) to an aromatic extraction unit (D) with sulfolane.
  • the paraffinic raffinate that circulates via the line (6) is sent partially to the gasoline pool via line (8) until an octane gasoline equal to or greater than the charge.
  • a cut with a boiling point ASTM D86 of 60 ° C desulphurated circulating via the line (5) is recovered at the top.
  • the effluent of the hydrodesulfurization flowing via line (4) is sent to an extraction of sulfolane aromatic.
  • the raffinate flowing via the line (6) is sent is sent partly to the gasoline pool via the line (8) to obtain an octane gasoline equal to or greater than the load.
  • the excess is sent to the steam cracker via line (7).
  • Extract (9) is sent to the essence pool.
  • the effluent of the hydrodesulfurization flowing via line (4) is sent to an extraction of sulfolane aromatic.
  • the raffinate flowing via the line (6) is sent is sent partly to the gasoline pool via the line (8) to obtain an octane gasoline equal to or greater than the load.
  • the excess is sent to the steam cracker via line (7).
  • Extract (9) is sent to the essence pool.
  • Raffinate is a good steam cracker feed and even better than in the previous example because it contains less olefins.
  • the effluent of the hydrodesulfurization flowing via the line (4) is sent to a sulfolane aromatic extraction (unit D).
  • the unit is identical to conventional aromatic extraction units.
  • the solvent / charge ratio is 6
  • the raffinate (7) is sent to steam cracking. Because of its almost completely paraffinic nature, it is an excellent steam cracker feedstock.
  • Extract (9) is sent to the essence pool.
  • the gasoline produced has an octane number which is very much improved with respect to the charge.
  • the effluent obtained at the end of the selective hydrogenation circulating via line (2) is then fractionated on a fractionation column (B). At the top of the column is recovered a section with a boiling point ASTM D86 of 60 ° C desulfurized circulating via the line (5).
  • the extraction raffinate circulating via the line (6) is then distilled.
  • the heaviest fraction (with a desulfurized ASTM D86 150-220 ° C distillation range) is sent to the diesel pool via line (13).
  • the light raffinate (having an ASTM D86 distillation endpoint of 150 ° C) flowing via the line (14) is partially sent to the gasoline pool (15) until an octane gasoline equal to or greater than the charge.
  • the cut with a distillation interval ASTM D86 150-220 will be sent to the diesel pool or kerosene with if necessary a hydrotreatment.
  • the light raffinate is a good load of steam cracker
  • the quantity of gasoline is also greatly reduced in favor of a better raffinate for petrochemicals.

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  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (8)

  1. Verfahren zum Herstellen einer Kohlenwasserstoffschnittes mit hoher Oktanzahl und niedrigem Schwefelgehalt ausgehend von einer Kohlenwasserstoffcharge, das mindestens die folgenden Schritte aufweist:
    - einen Schritt der selektiven Hydrogenierung der Diolefine der Kohlenwasserstoffcharge,
    - einen Schritt des Trennens des Abflusses, der bei dem Schritt der selektiven Hydrogenierung erzielt wird, der zu mindestens zwei Schnitten führt, eine Schnitt leichte Kohlenwasserstoffe und ein Schnitt schwere Kohlenwasserstoffe,
    - einen Schritt der ydrodesulfurierung des Schnittes schwere Kohlenwasserstoffe,
    - mindestens einen Schritt der Extraktion aromatischer Verbindungen an einem Teil oder dem vollständigen Abfluss, der von dem Hydrodesulfurierungsschritt stammt, wobei die Extraktion zu einem Raffinat, das mit Paraffinen im Vergleich zu der Charge angereichert ist, und zu einem Extrakt, der mit aromatischen Verbindungen angereichert ist, der zu einem Benzinpool geschickt wird, führt, bei dem der Schnitt leichte Kohlenwasserstoffe im Gemisch mit dem mit aromatischen Verbindungen angereicherten Extrakt und einem Teil des paraffinhaltigen Raffinats zu dem Benzinpool geschickt wird, und bei dem ein anderer Teil des paraffinhaltigen Raffinats zu einer Dampfcrackeinheit geschickt wird, um dort leichte Olefine zu erzeugen.
  2. Verfahren nach Anspruch 1, bei dem die Kohlenstoffwasserstoffcharge aus einer katalytischen Crackingeinheit oder einer thermischen Crackingeinheit oder einer Visbreaking-Einheit stammt.
  3. Verfahren nach eine der Ansprüche 1 oder 2, bei dem der Schritt der Wasserstoffentschwefelung selektiv ist, und in einem Schritt in eine oder zwei Reaktoren oder in zwei Schritten ausgeführt wird.
  4. Verfahren nach einem der Ansprüche 1 oder 2, bei dem der Schritt der Hydrodesulfurierung nicht selektiv ist.
  5. Verfahren nach Anspruch 1, bei dem wenigstens ein Teil des paraffinhaltigen Raffinats zu einem Trennungsschritt geschickt wird, der zu einem leichten Raffinat führt, das zu dem Benzinpool geschickt wird, gemischt mit dem Extrakt aromatischer Verbindungen, und zu einer Dampfcrackingeinheit, und zu einem schweren Raffinat, das zu dem Dieselpool oder zu dem Kerosinpool geschickt wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, bei dem der Trennungsschritt außerdem zu einem Zwischenkohlenwasserstoffschnitt führt, der als Charge zu dem Hydrodesulfurierungsschritt geschickt wird.
  7. Verfahren nach einem der Ansprüche 1 bis 6, bei dem der Schritt der Extraktion aromatischer Verbindungen eine Flüssig-Flüssig-Extraktion oder eine Extraktionsdestillation ist.
  8. Verfahren nach Anspruch 7, bei dem der Schritt der Extraktion der aromatischen Verbindungen eine Flüssig-Flüssig-Extraktion mit einem Lösemittelgehalt zwischen 1,5 und 5 ist.
EP10290246.7A 2009-05-26 2010-05-06 Verfahren zur Herstellung einer Kohlewasserstofffraktion mit hohem Oktan- und niedrigem Schwefelgehalt Active EP2256179B1 (de)

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JP2010275550A (ja) 2010-12-09
CN101899325B (zh) 2014-10-22
BRPI1001716A2 (pt) 2011-04-26
KR20100127726A (ko) 2010-12-06
KR101801975B1 (ko) 2017-11-27
ES2497541T3 (es) 2014-09-23
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US20100300932A1 (en) 2010-12-02
BRPI1001716B1 (pt) 2019-10-29

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