EP2816094A1 - Herstellungsverfahren einer Essenz mit niedrigem Schwefel- und Mercaptangehalt - Google Patents

Herstellungsverfahren einer Essenz mit niedrigem Schwefel- und Mercaptangehalt Download PDF

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Publication number
EP2816094A1
EP2816094A1 EP14305833.7A EP14305833A EP2816094A1 EP 2816094 A1 EP2816094 A1 EP 2816094A1 EP 14305833 A EP14305833 A EP 14305833A EP 2816094 A1 EP2816094 A1 EP 2816094A1
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EP
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Prior art keywords
gasoline
catalyst
weight
cut
treated
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EP14305833.7A
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English (en)
French (fr)
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EP2816094B1 (de
Inventor
Julien Gornay
Philibert Leflaive
Annick Pucci
Olivier TOUZALIN
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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Priority claimed from FR1355749A external-priority patent/FR3007416B1/fr
Priority claimed from FR1453795A external-priority patent/FR3020376B1/fr
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Publication of EP2816094A1 publication Critical patent/EP2816094A1/de
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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • 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
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/06—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial 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
    • 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
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/405—Limiting CO, NOx or SOx emissions
    • 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
    • C10G2300/70—Catalyst aspects
    • 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
    • C10G2300/80—Additives
    • 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

Definitions

  • the one that has been widely adopted consists in specifically treating the sulfur-rich gasoline bases by catalytic hydrodesulfurization processes in the presence of hydrogen.
  • the traditional processes desulphurize the species in a non-selective manner by hydrogenating a large part of the mono-olefins, which generates a strong loss in octane number and a high consumption of hydrogen.
  • the most recent processes such as the Prime G + (trade mark) process, make it possible to desulphurize the olefin-rich cracking species, while limiting the hydrogenation of the mono-olefins and consequently the octane loss and the high consumption. of hydrogen that results.
  • Such methods are for example described in patent applications EP 1077247 and EP 1174485 .
  • the process according to the invention may comprise a stage in which the effluent resulting from stage b) is mixed with a hydrocarbon fraction selected from a LPG (liquefied petroleum gas) section, a petrol fraction obtained from a distillation crude oil, a pyrolysis unit, a coker unit, a hydrocracking unit, an oligomerization unit and a C4 olefinic section, and the mixture is treated in step c ).
  • a hydrocarbon fraction selected from a LPG (liquefied petroleum gas) section
  • a petrol fraction obtained from a distillation crude oil
  • a pyrolysis unit a coker unit
  • a hydrocracking unit an oligomerization unit and a C4 olefinic section
  • the effluent resulting from stage c) is fractionated so as to separate an unreacted C4 olefinic section.
  • a gasoline distillation step is carried out so as to fractionate said gasoline in at least three light, medium and heavy gasoline cuts respectively and then the gasoline fraction is treated.
  • the heavy gasoline fraction resulting from the distillation is advantageously treated in a hydrodesulfurization step in a dedicated unit and then subjected to a mercaptan softening step after removal of the H 2 S.
  • the step softening of the desulphurised heavy gasoline fraction can be carried out either in a dedicated reactor or in the same softening reactor as that which processes the intermediate gasoline fraction (the intermediate and heavy cuts are treated in a mixture in a softening reactor) .
  • the process further comprises a step d) in which the effluent from step c) is sent to a fractionation column and a gasoline cutoff with a low mercaptan content is separated at the top of the fractionation column and a hydrocarbon cut containing thioether compounds at the bottom of the fractionation column.
  • the invention relates to a process for the treatment of essences comprising all types of chemical families and in particular diolefins, mono-olefins, and sulfur compounds.
  • the present invention finds particular application in the conversion of conversion gasolines, and in particular of gasoline from catalytic cracking, fluid-bed catalytic cracking (FCC), coking process, a visbreaking process, or a pyrolysis process.
  • gasoline from catalytic cracking units (FCC) contain, on average, between 0.5% and 5% by weight of diolefins, between 20% and 50% by weight of monoolefins, between 10 ppm and 0, 5% weight of sulfur
  • the desulfurization rate which depends on the sulfur content of the feedstock to be treated, is generally greater than 50% and preferably greater than 70% so that the product resulting from stage a) contains less than 100 ppm by weight. sulfur and preferably less than 50 ppm by weight of sulfur.
  • Any catalyst known to those skilled in the art capable of promoting the reactions of transformation of organic sulfur to H 2 S in the presence of hydrogen can be used within the scope of the invention.
  • the metal content of group VIII expressed as oxide is generally between 0.5% and 15% by weight, preferably between 1% and 10% by weight relative to the total weight of the catalyst.
  • the metal content of the Vlb group is generally between 1.5% and 60% by weight, preferably between 3% and 50% by weight relative to the total weight of the catalyst.
  • the catalyst is in a first activated step.
  • This activation can correspond either to calcination (oxidation) then to a reduction, or to a direct reduction, or to a calcination only.
  • the calcination step is generally carried out at temperatures ranging from 100 ° C. to 600 ° C. and preferably between 200 ° C. and 450 ° C. under an air flow rate.
  • the reduction step is performed under conditions to convert at least a portion of the oxidized forms of the base metal to metal. Generally, it consists in treating the catalyst under a flow of hydrogen at a temperature preferably of at least 300 ° C.
  • the catalyst comprises at least one element of group VIII (groups 8, 9 and 10 of the new periodic table Handbook of Chemistry and Physics, 76th Edition, 1995-1996 ), at least one element of group VIB (group 6 of the new periodic Handbook of Chemistry and Physics, 76th Edition, 1995-1996 ) and a support.
  • group VIII element is preferably chosen from nickel and cobalt and in particular nickel.
  • group VIB element is preferably selected from molybdenum and tungsten and very preferably molybdenum.
  • the gasoline to be treated is contacted with the catalyst at a temperature between 30 ° C and 250 ° C, and preferably between 60 ° C and 220 ° C, and even more preferably between 90 ° C and 200 ° C, with a liquid space velocity (LHSV) of between 0.5 h -1 and 10 h -1 , the unit of the liquid space velocity being the liter of filler per liter of catalyst and per hour (l / lh).
  • the pressure is between 0.2 MPa and 5 MPa, preferably between 0.5 and 2 MPa and even more preferably between 0.6 and 1 MPa.
  • step c the gasoline treated under the conditions set out above therefore has a reduced mercaptan content. Indeed, these have been converted into thioether type compounds whose molecular point is higher than the starting mercaptans.
  • the mercaptan softening step (step c) and the fractionation (step d) can be carried out simultaneously by means of a catalytic column equipped with a catalytic bed containing the softening catalyst.
  • the catalytic distillation column comprises two softening catalyst beds and the feed is fed into the column between the two catalyst beds.
  • the heavy cut resulting from the hydrodesulphurization catalytic distillation column may be treated in a second hydrodesulphurization unit, alone or in admixture with the heavy cut resulting from step d) of fractionation of the gasoline fraction.
  • light output from the catalytic distillation column hydrodesulfurization.
  • step c) In the case where step c) is carried out on the light cut, in order to improve the conversion ratio of the mercaptans (recombination) to thioether during step c), a mixture of a C 4 olefinic cut is advantageously carried out upstream of step c) with the light gasoline so that step c) is advantageously carried out on a mixture containing the light hydrocarbon cut and a C4 olefinic cut and not the light cut alone .
  • the mercaptan-sweetened effluent is sent to a separation column which separates an olefinic C4 cut and a softened soft cut into mercaptans.
  • the olefinic cut C4 withdrawn from the separation column is advantageously recycled to the reactor of step c).
  • the stabilized gasoline is sent via line 7 to a softening reactor 8 (step c) to reduce the mercaptan content of the stabilized gasoline.
  • the mercaptans contained in this stabilized gasoline are mainly recombination mercaptans resulting from the reaction of H 2 S on olefins.
  • the softening reactor uses a catalyst that makes it possible to carry out the addition reaction of the mercaptans to the olefins via a direct addition to the double bond to produce compounds of the thioether type, of formula R1-S -R2 with R1 and R2 being alkyl radicals, of molecular weight is higher than that of the starting mercaptan.
  • the catalytic conversion reaction of the mercaptans may be carried out optionally in the presence of hydrogen brought by line 9.
  • the separation column 15 used is equivalent to a debutanizer which separates at the top of the column 15 a C4 cut which is recycled in the softening reactor 8 via the line 16.
  • the bottom cut 17 recovered from the column 15 is divided in column 11 as described in the context of the figure 1 to provide a low sulfur and mercaptan light gasoline cut through line 12 and a heavy gasoline cut containing the thioether compounds formed in the softening reactor 8.
  • the intermediate intermediate section 13 may to be desulphurized in the hydrodesulfurization reactor 24 in admixture with the bottom cutoff 23 resulting from the first fractionation step carried out in column 20.
  • the heavy hydrocarbon fraction is then treated according to the process of the invention which consists of a hydrodesulfurization step carried out, in this embodiment, in a catalytic distillation column 45 comprising two beds of hydrodesulfurization catalysts 46.
  • the heavy hydrocarbon fraction is injected with hydrogen (via line 44) between the two hydrodesulphurization catalyst beds 46.
  • the catalytic distillation column 45 also makes it possible to fractionate the heavy hydrocarbon fraction into a intermediate head cup boiling in the range (C5-140 ° C) or (C5-160 ° C) and a bottom cut whose boiling temperature is greater than 140 ° C or 160 ° C respectively.
  • the softened intermediate mercaptan cut from reactor 8 may optionally undergo a stabilization step carried out in a stabilization column 31 from which a C4 - cut and a softened stabilized intermediate cut are extracted into mercaptans, respectively at the top and the bottom. bottom of said column 31.
  • the stabilized intermediate cut softened to mercaptans is then sent via line 33 to the fractionation column 11.
  • a hydrodesulfurization catalyst A is obtained by impregnation "without excess solution” of a transition alumina in the form of specific surface beads of 130 m 2 / g and a pore volume of 0.9 ml / g, with a aqueous solution containing molybdenum and cobalt in the form of ammonium heptamolybdate and cobalt nitrate respectively.
  • the catalyst is then dried and calcined under air at 500 ° C.
  • the cobalt and molybdenum content of this sample is 3% by weight of CoO and 10% by weight of MoO 3 .
  • the catalyst A 50 ml of the catalyst A are placed in a fixed-bed tubular hydrodesulfurization reactor.
  • the catalyst is first sulfided by treatment for 4 hours at a pressure of 3.4 MPa at 350 ° C., in contact with a feedstock consisting of 2% by weight of sulfur in the form of dimethyl disulphide in n-heptane.
  • the treated feed C1 is a catalytic cracked gasoline whose initial boiling point is 55 ° C, the end point is 242 ° C, whose MON is 79.8 and the RON is 89.5. Its sulfur content is 359 ppm by weight.
  • This feed is treated on catalyst A, under a pressure of 2 MPa, with a volume ratio of hydrogen on feedstock to be treated (H 2 / HC) of 360 l / l and a space velocity (VVH) of 4 h -1 .
  • H 2 / HC volume ratio of hydrogen on feedstock to be treated
  • VVH space velocity
  • the gasoline A1 as obtained and described in Example 1 is treated in the absence of hydrogen on the demercattering catalyst B, at a pressure of 1 MPa, a VVH of 3 h -1 and a temperature of 100 ° C. After treatment, the gasoline B1 obtained is cooled.
  • a catalyst D is obtained by impregnation of a surface alumina of 239 m 2 / g and a pore volume of 0.6 ml / g, with an aqueous solution containing molybdenum and nickel. The catalyst is then dried and calcined under air at 500 ° C. The nickel and molybdenum content of this sample is 9.5% by weight of NiO and 13% by weight of MoO 3 .
  • Gasoline A1 as obtained and described in Example 1 is mixed with a C2 charge to obtain a C3 charge.
  • Charge C2 is a light cracked gasoline which has undergone selective hydrogenation of diolefins, having an initial boiling point of 22 ° C and an end point of 71 ° C, of which MON is 82.5 and RON is 96.9. Its sulfur content is 20 ppm by weight, its mercaptan content is less than 3 ppm by weight and its olefin content is 56.7% by weight.
  • the charge C3 is obtained by mixing 80% by weight of gasoline A1 with 20% by weight of charge C2.
  • the resulting mixture is a gasoline with an initial boiling point of 22 ° C and an end point of 242 ° C. Its sulfur content is 73 ppm, its mercaptan content is 19 ppm by weight and its olefin content is 31% by weight.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
EP14305833.7A 2013-06-19 2014-06-02 Herstellungsverfahren einer essenz mit niedrigem schwefel- und mercaptangehalt Active EP2816094B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1355749A FR3007416B1 (fr) 2013-06-19 2013-06-19 Procede de production d'une essence a basse teneur en soufre et en mercaptans
FR1453795A FR3020376B1 (fr) 2014-04-28 2014-04-28 Procede de production d'une essence a basse temperature en soufre et en marcaptans.

Publications (2)

Publication Number Publication Date
EP2816094A1 true EP2816094A1 (de) 2014-12-24
EP2816094B1 EP2816094B1 (de) 2020-04-29

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Country Status (6)

Country Link
US (1) US9957448B2 (de)
EP (1) EP2816094B1 (de)
KR (1) KR102322556B1 (de)
CN (1) CN104232156B (de)
BR (1) BR102014014718B1 (de)
RU (1) RU2665701C2 (de)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016165853A1 (fr) * 2015-04-15 2016-10-20 IFP Energies Nouvelles Procede d'adoucissement en composes du type sulfure d'une essence olefinique
FR3057578A1 (fr) * 2016-10-19 2018-04-20 IFP Energies Nouvelles Procede d'hydrodesulfuration d'une essence olefinique.
EP3498370A1 (de) * 2017-12-14 2019-06-19 IFP Energies nouvelles Katalysator für die selektive wasserstoffentschwefelung von fcc-benzinen
WO2021013528A1 (fr) * 2019-07-23 2021-01-28 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans
WO2021185658A1 (fr) * 2020-03-20 2021-09-23 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans

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FR3049955B1 (fr) * 2016-04-08 2018-04-06 IFP Energies Nouvelles Procede de traitement d'une essence
FR3056599B1 (fr) * 2016-09-26 2018-09-28 IFP Energies Nouvelles Procede de traitement d'une essence par separation en trois coupes.
FR3099173B1 (fr) * 2019-07-23 2021-07-09 Ifp Energies Now Procédé de production d'une essence a basse teneur en soufre et en mercaptans

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Cited By (14)

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Publication number Priority date Publication date Assignee Title
WO2016165853A1 (fr) * 2015-04-15 2016-10-20 IFP Energies Nouvelles Procede d'adoucissement en composes du type sulfure d'une essence olefinique
FR3035117A1 (fr) * 2015-04-15 2016-10-21 Ifp Energies Now Procede d'adoucissement en composes du type sulfure d'une essence olefinique
US10822555B2 (en) 2015-04-15 2020-11-03 IFP Energies Nouvelles Method for sweetening an olefinic petrol of sulphide-type compounds
US10377956B2 (en) 2016-10-19 2019-08-13 IFP Energies Nouvelles Process for hydrodesulphurizing an olefinic gasoline
EP3312260A1 (de) * 2016-10-19 2018-04-25 IFP Energies nouvelles Verfahren zur hydroentschwefelung einer olefinischen essenz
FR3057578A1 (fr) * 2016-10-19 2018-04-20 IFP Energies Nouvelles Procede d'hydrodesulfuration d'une essence olefinique.
EP3498370A1 (de) * 2017-12-14 2019-06-19 IFP Energies nouvelles Katalysator für die selektive wasserstoffentschwefelung von fcc-benzinen
FR3075072A1 (fr) * 2017-12-14 2019-06-21 IFP Energies Nouvelles Catalyseur d'hydrodesulfuration selective des essences de fcc.
US11034894B2 (en) 2017-12-14 2021-06-15 IFP Energies Nouvelles Hydrodesulphurization catalyst selective of gasolines from FCC
WO2021013528A1 (fr) * 2019-07-23 2021-01-28 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans
FR3099175A1 (fr) * 2019-07-23 2021-01-29 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans
US12054679B2 (en) 2019-07-23 2024-08-06 IFP Energies Nouvelles Method for producing gasoline with low sulphur and mercaptan content
WO2021185658A1 (fr) * 2020-03-20 2021-09-23 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans
FR3108333A1 (fr) * 2020-03-20 2021-09-24 IFP Energies Nouvelles Procédé de production d'une essence a basse teneur en soufre et en mercaptans

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RU2014124384A (ru) 2015-12-27
US20140374315A1 (en) 2014-12-25
US9957448B2 (en) 2018-05-01
BR102014014718A2 (pt) 2015-06-02
EP2816094B1 (de) 2020-04-29
KR20140147737A (ko) 2014-12-30
RU2665701C2 (ru) 2018-09-04
CN104232156B (zh) 2018-12-07
KR102322556B1 (ko) 2021-11-04
BR102014014718B1 (pt) 2021-02-09

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