EP1396532B1 - Procédé de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge - Google Patents

Procédé de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge Download PDF

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Publication number
EP1396532B1
EP1396532B1 EP03292157A EP03292157A EP1396532B1 EP 1396532 B1 EP1396532 B1 EP 1396532B1 EP 03292157 A EP03292157 A EP 03292157A EP 03292157 A EP03292157 A EP 03292157A EP 1396532 B1 EP1396532 B1 EP 1396532B1
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EP
European Patent Office
Prior art keywords
cut
process according
hydrocarbons
weight
fraction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP03292157A
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German (de)
English (en)
French (fr)
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EP1396532A1 (fr
Inventor
Patrick Briot
Vincent Coupard
Alain Forstière
Thierry Poussereau
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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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon 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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation

Definitions

  • the present invention relates to a method of upgrading a liquid hydrocarbon feed, typically a gasoline cut.
  • the method according to the present invention not only makes it possible to enhance said charge by decreasing its vapor pressure but also to produce a synthetic kerosene having a high smoke point.
  • the initial hydrocarbon feedstock comprises at least in part a C5 cut, that is to say predominantly comprising molecules containing 5 carbon atoms.
  • said liquid hydrocarbon feed is a gasoline cut resulting from a steam cracking, catalytic cracking (FCC) or coking process.
  • the C5 fraction contained in hydrocarbons is currently used for the most part directly as a gasoline base although it has a low octane number.
  • a known alternative allowing a better valuation of said cut resides in its use as a petrochemical intermediate.
  • the C5 fraction is generally separated from the other hydrocarbons by a depentanizer. It is therefore an important source of olefins and diolefins with a variety of uses: resins, elastomers and specialty products.
  • the estimated requirements for this application will be approximately 1.5 Mt (million tonnes) in 2005.
  • the availability in C5 cut for the only part resulting from steam cracking is about 5 Mt in 1995. Therefore, it appears that the C5 hydrocarbon requirements for petrochemicals are currently largely met and the surplus available portion must be used in gasolines, despite its low octane number, as indicated above.
  • US-A-5,326,466 discloses a process comprising contacting a fraction comprising pentenes with a hydrocarbon fraction comprising benzene in the presence of a catalyst promoting the oligomerization and alkylation reactions, followed by the separation of a petrol cut, comprising the majority of products from the alkylation and dimerization reactions.
  • OIL & GAS JOURNAL, vol. 90, no. 7, 1992, 72-74 discloses a process comprising the separation from a hydrocarbon feed of a fraction comprising pentenes, followed by oligomerization and alkylation of pentenes and finally the separation of a cut of gasoline, in order to reduce the vapor pressure of this liquid hydrocarbon feedstock and to recover at least a portion of the low octane C5 fraction contained in these same hydrocarbons.
  • the present invention proposes itself to provide an alternative method for processing and recovering large and increasing amounts of said C5 cut.
  • One of the objects of the present invention is a new scheme of recovery process such a cut to allow to process much larger amounts of said cut that petrochemical processes previously described.
  • the present invention also proposes to provide a solution making it possible to reduce the Reid vapor pressure of a charge of liquid hydrocarbons, for example gasolines, while proposing an alternative solution making it possible to valorize at least a part, even the totality of the low octane C5 fraction contained in these same hydrocarbons.
  • said fraction (O1) comprises at least 30% by weight of compounds containing 5 carbon atoms, preferably at least 50% by weight and of very preferably at least 70% by weight of compounds containing 5 carbon atoms.
  • said fraction may, without departing from the scope of the invention, contain amounts of C5 hydrocarbons greater than 90% by weight, preferably greater than 95% by weight, and very preferably higher than 99% weight.
  • said hydrocarbon feed (O1) comprises at least 10% by weight of pentenes, preferably at least 30% by weight, and very preferably at least 50% by weight of pentenes.
  • the method according to the invention thus makes it possible on the one hand to enhance said hydrocarbon feed, for example a gasoline cut, by separating, most often by distillation, all or part of the C5 fraction contained therein. and on the other hand to obtain a fuel whose demand is growing: kerosene, by dimerization reaction and alkylation of said C5 cut with a cut (O2) as previously described.
  • Said cut (O2) is advantageously derived from another refinery process, and is preferably selected from the group consisting of gasoline from a catalytic cracking (FCC) process, the products resulting from the oligomerization of the ethylene, dehydrogenation of paraffins, dimerization and / or oligomerization of butenes and propenes such as the Dimersol® process (see also Hydrocarbon Processing, Vol 89, pp 143-149, (1980) and Vol 91 pp. 110-112 (1982)).
  • FCC catalytic cracking
  • a cut (O2) comprising at least 30% by weight of hydrocarbons containing from 6 to 10 carbon atoms, preferably at least 50% by weight of hydrocarbons containing from 6 to 10, will be chosen to promote a good yield of kerosene. carbon atoms and very preferably at least 70% by weight of hydrocarbons containing from 6 to 10 carbon atoms. It was found by the applicant that the properties of the kerosene cut ( ⁇ ) obtained and particularly its smoke point are all the more interesting that the amount of olefins present in said hydrocarbon cut (O2) is greater.
  • the hydrocarbon feed (O2) comprises at least 10% by weight of olefins, preferably at least 30% by weight of olefins and very preferably at least 50% by weight of olefins.
  • a significant improvement in the smoke point of kerosene produced and / or the elimination of any sulfur impurities contained in the kerosene fraction is advantageously obtained by implementing an additional step d) of hydrogenating the unsaturated compounds contained in the kerosene fraction ( ⁇ ) resulting from step c) of the process according to the invention.
  • the smoke point is a standardized test that measures the maximum height of a flame that does not emit smoke in a kerosene lamp (wick lamp).
  • the smoke point is expressed in mm. The higher the smoke point, indicating a lower C / H ratio, the better the qualities of kerosene.
  • said section (O2) consists exclusively of an olefin or a mixture of olefins, that is to say constituted by a pure olefin or a mixture of pure olefins .
  • the upper (final) distillation point of the petrol fraction ( ⁇ ) is less than 100 ° C. and the lower (initial) distillation point of the kerosene fraction ( ⁇ ) is from at least 100 ° C, preferably above 120 ° C and very preferably above 150 ° C.
  • the catalyst for the dimerization and alkylation reactions of olefins is an acidic catalyst such as for example described in US Pat. No. 4,902,847. It is preferably selected from the group consisting of silica, silica-aluminas, silicoaluminates, titanosilicates, zirconia-silicas, mixed alumina-titanium, zeolites, clays, ion exchange resins, mixed oxides.
  • a particular embodiment of the invention may consist in using a physical mixture of at least two catalysts such as those mentioned above in proportions varying from 95/5 to 5/95, preferably 85/15 to 15/85, and very preferentially 70/30 to 30/70. It is also possible to use supported sulfuric acid or phosphoric acid. In this case the support is usually a support mineral such as for example one of those mentioned above and more particularly silica, alumina or a silica-alumina.
  • steps b) and c) can be carried out simultaneously, for example using reactors placed in parallel or in a catalytic distillation column.
  • At least a fraction of at least one gasoline cut resulting from step c) constitutes at least in part the hydrocarbon cut (O2) of step b) of setting in touch.
  • the gasoline cuts from step c) can be used as a gasoline base.
  • This section ( ⁇ ) or kerosene may subsequently be optionally hydrogenated in a unit C after mixing with a gas containing hydrogen and supplied via line 6.
  • Said hydrogenation is intended to eliminate any sulfur impurities and / or significantly improve the smoke point of kerosene produced.
  • Examples 1 and 2 make it possible to understand the reaction mechanisms involved on model molecules and Examples 3 and 4 use a process each using a feedstock derived from a refinery process.
  • the smoke point of this section measured according to ASTM D1322, is 25 mm.
  • the method according to the invention thus makes it possible to upgrade light petrol cuts by producing, mainly from said cups, a synthetic kerosene with a high smoke point, that is to say much higher than current specifications.

Landscapes

  • 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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Electrostatic Separation (AREA)
  • Treatment Of Fiber Materials (AREA)
  • Gas Separation By Absorption (AREA)
EP03292157A 2002-09-04 2003-09-03 Procédé de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge Expired - Lifetime EP1396532B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0210951 2002-09-04
FR0210951A FR2843969B1 (fr) 2002-09-04 2002-09-04 Procede de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge

Publications (2)

Publication Number Publication Date
EP1396532A1 EP1396532A1 (fr) 2004-03-10
EP1396532B1 true EP1396532B1 (fr) 2006-05-17

Family

ID=31503110

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EP03292157A Expired - Lifetime EP1396532B1 (fr) 2002-09-04 2003-09-03 Procédé de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge

Country Status (11)

Country Link
US (1) US7161052B2 (da)
EP (1) EP1396532B1 (da)
JP (1) JP4446229B2 (da)
KR (1) KR100982709B1 (da)
AT (1) ATE326515T1 (da)
DE (1) DE60305254T2 (da)
DK (1) DK1396532T3 (da)
ES (1) ES2263930T3 (da)
FR (1) FR2843969B1 (da)
MY (1) MY135344A (da)
PT (1) PT1396532E (da)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8128879B2 (en) 2010-03-31 2012-03-06 Uop Llc Apparatus for increasing weight of olefins
US8471084B2 (en) 2010-03-31 2013-06-25 Uop Llc Process for increasing weight of olefins
FR2975103B1 (fr) 2011-05-12 2014-08-29 IFP Energies Nouvelles Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone
FR3134110A1 (fr) 2022-04-05 2023-10-06 Axens Procédé amélioré de production de distillats moyens par oligomérisation d’une charge oléfinique

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2684325A (en) * 1951-12-26 1954-07-20 Universal Oil Prod Co Production of saturated gasolines with increased antiknock properties
US5326466A (en) * 1991-01-22 1994-07-05 Mobil Oil Corporation Distillate dewaxing reactor system integrated with olefin upgrading
US5059741A (en) 1991-01-29 1991-10-22 Shell Oil Company C5/C6 isomerization process
US5684220A (en) 1995-03-23 1997-11-04 Phillips Petroleum Company Process for reducing the vapor pressure of gasoline by removing amylenes therefrom and enhancing the octane thereof
CA2205812C (en) 1995-10-02 2004-03-23 Nkk Corporation Scrap melting process
US6059962A (en) * 1998-09-09 2000-05-09 Bp Amoco Corporation Multiple stage sulfur removal process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
OIL AND GAS JOURNAL, vol. 90, no. 7, 17 February 1992 (1992-02-17), Tulsa, Okla., US, pages 72 - 74 *

Also Published As

Publication number Publication date
DE60305254T2 (de) 2006-09-14
JP2004099891A (ja) 2004-04-02
KR20040021552A (ko) 2004-03-10
US20050101821A1 (en) 2005-05-12
KR100982709B1 (ko) 2010-09-17
JP4446229B2 (ja) 2010-04-07
PT1396532E (pt) 2006-09-29
MY135344A (en) 2008-03-31
ES2263930T3 (es) 2006-12-16
DK1396532T3 (da) 2006-09-18
FR2843969A1 (fr) 2004-03-05
US7161052B2 (en) 2007-01-09
FR2843969B1 (fr) 2007-03-23
DE60305254D1 (de) 2006-06-22
ATE326515T1 (de) 2006-06-15
EP1396532A1 (fr) 2004-03-10

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