US20120103867A1 - Process for the production of kerosene and diesel fuels from light unsaturated fractions and btx-rich aromatic fractions - Google Patents

Process for the production of kerosene and diesel fuels from light unsaturated fractions and btx-rich aromatic fractions Download PDF

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US20120103867A1
US20120103867A1 US13/225,589 US201113225589A US2012103867A1 US 20120103867 A1 US20120103867 A1 US 20120103867A1 US 201113225589 A US201113225589 A US 201113225589A US 2012103867 A1 US2012103867 A1 US 2012103867A1
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Vincent Coupard
Annick Pucci
Quentin Debuisschert
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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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
    • 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
    • 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
    • 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
    • C10G67/06—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 including a sorption process as the refining step 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
    • 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
    • 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
    • C10G69/08—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 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • 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
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • 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

Definitions

  • This invention proposes an attractive approach that makes it possible, starting from light cracked naphtha (optionally including any proportion of olefinic fractions C3 and C4 called “LPG”), and a BTX-rich aromatic fraction, to answer an increased demand for diesel fuel and kerosene, without involving new and expensive hydrocracking units.
  • LPG light cracked naphtha
  • BTX-rich aromatic fraction a BTX-rich aromatic fraction
  • This approach can be defined as an alternative to the “hydrocracking” approach, relying on an oligomerization of light olefins of 3 to 10 carbon atoms, in a preferred manner 4 to 6 carbon atoms, coupled to an alkylation of olefins of 8 to 10 carbon atoms, not having reacted to the oligomerization on a BTX-rich fraction, generally available starting from a semi-regenerative or regenerative reforming.
  • This alkylation culminates in a fraction that is located in the range of middle distillates (diesel fuel or kerosene) that it is then necessary to hydrotreat and/or hydrogenate to culminate in commercial products.
  • middle distillates diesel fuel or kerosene
  • FIG. 1 is a schematic representation of one embodiment of the invention.
  • This invention describes a process for the production of diesel fuel ( 13 ) from a gasoline fraction ( 1 ) that originates from a catalytic cracking unit and a BTX fraction ( 9 ) that originates from a unit for catalytic reforming of gasolines, relying on the concatenation of the following stages:
  • the gasoline fraction that constitutes the feedstock ( 1 ) is generally a catalytic cracking gasoline that contains 5 to 10 carbon atoms and in a preferred manner 5 to 7 carbon atoms.
  • the acid catalyst treatment (TR) stage 2 relies on an ion-exchange resin-type acid catalyst, or supported phosphoric acid catalyst, or any acid catalyst previously used in the downstream stages of oligomerization (OLG) or alkylation (ALK) in a temperature range of 20° C. to 350° C., in a preferred manner 40° C. to 250° C., and in a pressure range of 1 bar to 100 bar, in a preferred manner 10 to 30 bar, and in a VVH range of 0.1 h-1 to 5 h-1, in a preferred manner 0.3 h-1 to 2.0 h-1.
  • OLG oligomerization
  • ALK alkylation
  • VVH refers to the ratio between the volumetric flow rate of feedstock and the volume of catalyst.
  • the oligomerization stage 4 is supplied by the cracking gasoline ( 4 ) and an LPG fraction that contains olefins and works on a preferably zeolitic- or silica alumina-type acid catalyst in a temperature range of 20° C. to 400° C., in a preferred manner from 100° C. to 350° C., and in a pressure range of 1 to 100 bar, in a preferred manner 20 to 70 bar, and in a VVH range of 0.1 h-1 to 5 h-1, in a preferred manner 0.2 h-1 to 1.0 h-1.
  • alkylation stage 5 is supplied by the effluent ( 8 ) of the oligomerization (OLG) unit and by a fraction that is rich in aromatic compounds ( 9 ) containing 6 to 12 carbon atoms, and in an also preferred manner 6 to 9 carbon atoms, and it works on a preferably zeolitic- or silicoaluminate-type acid catalyst, in a temperature range of 20° C. to 400° C., in a preferred manner 100° C.
  • the hydrotreatment (HDT) stage 6 uses a catalyst that contains at least one metal that is selected from among Ni, Co and Mo and operates in a temperature range of 50° C. to 400° C., in a preferred manner 100° C. to 350° C., and in a pressure range of 1 bar to 100 bar, in a preferred manner 20 bar to 70 bar, and in a VVH range of 0.1 h-1 to 10 h-1, in a preferred manner 0.5 h-1 to 5.0 h-1.
  • the hydrotreatment (HDT) stage 6 uses a catalyst that contains at least one metal that is selected from among Pd and Pt and operates in a temperature range of 50° C. to 300° C., in a preferred manner from 100° C. to 250° C., and in a pressure range of 1 bar to 100 bar, in a preferred manner from 20 bar to 70 bar, and in a VVH range of 0.1 h-1 to 10 h-1, in a preferred manner from 0.5 h-1 to 5.0 h-1.
  • stage 2 for acid catalyst treatment is preceded by a selective hydrogenation (SHU) stage 1 of the initial gasoline fraction.
  • This invention describes a process for producing kerosene or diesel fuel from olefinic fractions that are typically obtained from a unit for catalytic cracking of gasolines (denoted FCC in abbreviated form) and a BTX-rich fraction (abbreviation of benzene, toluene, xylene) typically obtained from a semi-regenerative or regenerative reforming unit, generally present on the same site as the FCC unit.
  • FCC catalytic cracking of gasolines
  • BTX-rich fraction abbreviation of benzene, toluene, xylene
  • the olefinic fraction can also originate from steam-cracking-type units (denoted SC in abbreviated form), Fischer-Tropsch synthesis units (denoted FT in abbreviated form), coking units (denoted CK in abbreviated form), or else a visco-reduction unit (denoted VB in abbreviated form).
  • the BTX-rich fraction can also originate from a steam-cracking (SC) unit, a vaporeforming unit (denoted VR in abbreviated form), an olefin cracking unit (denoted CO in abbreviated form), or else a unit that transforms methanol into olefins (denoted MTO in abbreviated form).
  • the feedstock to be treated ( 1 ) is a distillation interval gasoline that is between 30° C. and 250° C.
  • This feedstock is optionally sent into an SHU unit that makes it possible to hydrogenate the gum-generating unsaturated hydrocarbons selectively, such as the diolefins.
  • the treated effluent ( 2 ) is sent directly or after distillation into a treatment (TR) unit that is based on the use of an acid catalyst, preferably an ion-exchange resin-type catalyst as described in the patent FR 2,840,620, or of the supported phosphoric acid type.
  • a treatment (TR) unit that is based on the use of an acid catalyst, preferably an ion-exchange resin-type catalyst as described in the patent FR 2,840,620, or of the supported phosphoric acid type.
  • This stage has as its object to capture compounds that poison the acid catalysts, in particular the nitrogen-containing compounds, and optionally to transform them into heavier compounds.
  • the effluent ( 3 ) of the unit for treatment with resins (TR) is sent into a distillation column (CD 1 ) from which 3 fractions are extracted:
  • This type of unit is, for example, the unit known commercially under the name of Prime G+, marketed by the AXENS Company, whose description can be found in the patent FR 2,797,639.
  • OLG oligomerization
  • this stream ( 7 ) is:
  • the oligomerization (OLG) unit preferably operates on a zeolitic- or silica-alumina-type acid catalyst, in a temperature range of 20° C. to 400° C., in a preferred manner 100° C. to 350° C., and in a pressure range of 1 bar to 100 bar, in a preferred manner 20 bar to 70 bar, and in a VVH range of 0.1 h-1 to 5 h-1, in a preferred manner 0.2 h-1 to 1.0 h-1.
  • the light olefin fraction with a boiling point that is less than 150° C., not having reacted in the oligomerization (OLG) unit, constitutes the stream ( 8 ) that supplies the alkylation (ALK) unit that relies on a BTX fraction ( 9 ) that is generally obtained from a regenerative reforming unit of the gasolines.
  • the unit for alkylation of olefins ( 8 ) obtained from the oligomerization (OLG) unit on the BTX fraction ( 9 ) preferably operates on a zeolitic- or silicoaluminate-type acid catalyst in a temperature range of 20° C. to 400° C., in a preferred manner 100° C. to 350° C., and in a pressure range of 1 bar to 100 bar, in a preferred manner 20 bar to 70 bar, and in a VVH range of 0.05 h-1 to 5 h-1, in a preferred manner 0.1 h-1 to 2.0 h-1.
  • the effluent ( 11 ) of the alkylation (ALK) unit is sent into a distillation column (CD 2 ) from which 3 fractions are extracted:
  • the starting material is a feedstock that consists of a catalytic cracking gasoline and a BTX fraction that originates from a catalytic reforming unit.
  • An LPG fraction that originates from the catalytic cracking unit is also added.
  • the mass flow rates of the components of the feedstock are as follows:
  • the gasoline ( 1 ) is introduced into a selective hydrogenation unit (SHU) that operates under the following conditions:
  • the hydrogenated gasoline ( 2 ) is introduced in an acid catalyst treatment (TR) unit that operates under the following conditions:
  • the effluent ( 3 ) of the TR unit is introduced into a distillation column (CD 1 ) from which the following are separated:
  • the top fraction ( 4 ) is mixed with a certain quantity of the LPG fraction ( 10 ), and the resulting mixture is introduced into the oligomerization (OLG) unit that operates under the following conditions:
  • the oligomerization (OLG) unit produces, on the one hand, an effluent ( 7 ) that consists of oligomerized olefins and that is sent in part ( 7 a ) in a mixture with the bottom fraction ( 6 ) of the distillation column (CD 1 ) into a hydrotreatment (HDT) unit that operates under the following conditions:
  • the effluent ( 12 ) of the hydrogenation (HDT) unit is sent to the total hydrogenation (HT) unit, optionally mixed with the part ( 7 b ) of the olefinic effluent ( 7 ).
  • the effluent ( 13 ) of the total hydrogenation (HT) unit constitutes the production of desired diesel fuel with the following specifications:
  • the intermediate effluent ( 5 ) of the distillation column CD 1 is sent to the gasoline pool.
  • the oligomerization (OLG) unit also produces an effluent ( 8 ) of olefins in C3 and C4 that is sent with the BTX fraction ( 9 ) into an alkylation (ALK) unit that works under the following conditions:
  • the effluent ( 11 ) of the alkylation (ALK) unit is sent into a second distillation column (CD 2 ) that produces at the bottom an effluent ( 11 c ) that is sent into the total hydrogenation (HT) unit and therefore contributes to the production of the desired diesel fuel ( 13 ).
  • the lateral effluent ( 11 b ) of the distillation column (CD 2 ) is sent to the alkylation (ALK) unit.
  • the top effluent ( 11 a ) of the column CD 2 is sent to the gasoline pool.
  • Tables A and B below provide the detail of streams according to the diagram of FIG. 1 .
  • the process according to the invention therefore produced 66 tons/hour of diesel fuel ( 13 ), starting from 100 tons/hour of FCC gasoline ( 1 ), 18 tons/hour of BTX fraction ( 9 ), and 25 t/h of the LPG fraction of FCC ( 10 ), or a yield ( 13 )/( 1 )+( 9 )+( 10 ) of 46% transformation of a gasoline fraction into a distillate fraction, usable as a base of kerosene or diesel fuel.
  • Cn refers to a paraffinic fraction with n carbon atoms
  • Cn refers to an olefinic fraction with n carbon atoms
  • A refers to aromatic compounds
  • T refers to toluene
  • X refers to xylenes
  • indices n, i, and c respectively mean normal (or linear), iso (or branched) and cyclic.

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US13/225,589 2010-09-07 2011-09-06 Process for the production of kerosene and diesel fuels from light unsaturated fractions and btx-rich aromatic fractions Abandoned US20120103867A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1003559A FR2964389A1 (fr) 2010-09-07 2010-09-07 Procede de production de carburants kerosene et diesel a partir de coupes insaturees legeres et de coupes aromatiques riches en btx
FR10/03.559 2010-09-07

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US20130211161A1 (en) * 2012-02-15 2013-08-15 IFP Energies Nouvelles Process for converting a heavy feed using a catalytic cracking unit and a step for selective hydrogenation of the gasoline obtained from catalytic cracking
WO2014109766A1 (fr) * 2013-01-14 2014-07-17 Badger Licensing Llc Procédé d'équilibrage entre la production d'essence et de distillat dans une raffinerie

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CN104711022B (zh) * 2013-12-16 2016-11-16 中国石油化工股份有限公司 一种增加汽油收率生产超低硫汽油的两段催化汽油改质方法

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US7601254B2 (en) * 2005-05-19 2009-10-13 Uop Llc Integrated fluid catalytic cracking process
US20110147263A1 (en) * 2009-12-18 2011-06-23 Exxonmobil Research And Engineering Company Process and system to convert olefins to diesel and other distillates

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