EP1436362B1 - Verfahren zur hydrodesulfurierung mit einer strippung und einer fraktionierung - Google Patents

Verfahren zur hydrodesulfurierung mit einer strippung und einer fraktionierung Download PDF

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EP1436362B1
EP1436362B1 EP02774912A EP02774912A EP1436362B1 EP 1436362 B1 EP1436362 B1 EP 1436362B1 EP 02774912 A EP02774912 A EP 02774912A EP 02774912 A EP02774912 A EP 02774912A EP 1436362 B1 EP1436362 B1 EP 1436362B1
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EP
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Prior art keywords
section
hydrodesulphurisation
fraction
stripping
vacuum
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EP02774912A
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French (fr)
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EP1436362A1 (de
EP1436362B2 (de
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Renaud Galeazzi
Alain Dunet
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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
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/22—Separation of effluents
    • 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
    • C10G2300/1048—Middle distillates
    • C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °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
    • C10G2300/1074—Vacuum distillates
    • 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
    • C10G2300/201—Impurities
    • C10G2300/207—Acid gases, e.g. H2S, COS, SO2, HCN
    • 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
    • C10G2300/4081—Recycling 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4093—Catalyst stripping
    • 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
    • C10G2400/06—Gasoil

Definitions

  • the patent US 3,733260 discloses a process for the hydrodesulphurisation of gas oils comprising a hydrodesulfurization reaction section, a separation of the effluent of this section into a gaseous fraction and a first high temperature and high pressure liquid fraction, a partial condensation of the said vapor phase into a fraction comprising essentially hydrogen and a second liquid fraction, stripping of the H 2 S and light hydrocarbons of the first and second liquid fractions by means of the previously treated hydrogen, separation of the stripped hydrocarbons into a naphtha and a diesel fuel and recycling said naphtha to the condensation stage.
  • the patent application WO 98/42804 discloses a composition comprising paraffinic, naphthenic and alkylbenzene fractions and processes for producing such composition.
  • One of the processes described comprises a heavy molecule cracking reactor in the presence of hydrogen followed by a gas / liquid separation, a stripping and a vacuum fractionation after reheating the stripped effluent by means of an oven .
  • the patent US 4,808,289 discloses a process for hydrotreating residues comprising mixing said residue with lighter hydrocarbons from a separator flask, sending said mixture to a series of reactors operated as a bubbling bed, separating in a separator flask from effluent obtained in 2 gaseous and liquid fractions, the fractionation of the liquid in an atmospheric distillation tower into a naphtha and a residue, then a vacuum fractionation of this residue into a gas, a naphtha and a vacuum residue
  • the present invention relates to a process for hydrodesulfurization of gas oil or vacuum distillate, preferably vacuum gas oil and / or vacuum distillates, comprising at least one hydrodesulfurization reaction section, at least one stripping section and at least one a fractionation section in which the main fractionation column is operated under a moderate vacuum.
  • the method according to the invention makes it possible to reduce the amount of heat to be supplied to the charge of the fractionation section and thus to operate said section at moderate temperature levels.
  • the method according to the invention therefore makes it possible to desulphurize a gas oil and or a vacuum distillate without the need to implant a furnace between the stripping section and the fractionation section, which represents a significant economic advantage over the processes of the prior art.
  • the present invention relates to a method and a facility for hydrodesulfurization of gas oil or vacuum distillate, preferably vacuum gas oil and / or vacuum distillates, comprising at least one hydrodesulfurization reaction section, at least one stripping section. and at least one fractionation section in which the main fractionating column is operated under a moderate vacuum.
  • the installation according to the invention also comprises a hot separator flask.
  • the hydrodesulfurization reaction section may comprise one or more reactors arranged in series or in parallel, for example two reactors arranged in series.
  • Each reactor of the reaction section comprises at least one catalyst bed.
  • the catalyst can be used in fixed bed or expanded bed, or in bed bubbly. In the case of a catalyst implemented in fixed bed, it is possible to have several catalyst beds in at least one reactor.
  • Any catalyst known to those skilled in the art can be used in the process according to the invention, for example a catalyst comprising at least one element selected from the elements of Group VIII of the periodic table (Groups 8, 9 and 10 of the new periodic classification) and possibly at least one element selected from Group VIB elements of the Periodic Table (Group 6 of the new Periodic Table).
  • the temperature is typically between about 200 and about 460 ° C.
  • the total pressure is typically between about 1 MPa and about 20 MPa, typically between 2 and 20 MPa, preferably between 2.5 and 18 MPa, and most preferably between 3 and 18 MPa.
  • the overall hourly space velocity of liquid charge for each catalytic step is typically from about 0.1 to about 12, and generally from about 0.4 to about 10.
  • the purity of the hydrogen used in the process according to the invention is typically between 50 and 99.9.
  • the amount of hydrogen relative to the liquid feed is typically from about 50 to about 1200 Nm3 / m3.
  • the fractionation and stripping sections may be equipped with any type of stripping column at any pressure or moderate vacuum fractionation known to those skilled in the art.
  • the stripping can be carried out by means of any stripping gas such as for example a gas containing hydrogen or steam.
  • steam is used to carry out said stripping.
  • the vacuum column is also preferably fed by means of any stripping gas, preferably steam.
  • the additional heat necessary for this vaporization may possibly be provided by increasing the temperature of said separator flask with respect to the current practice which corresponds to a temperature generally of between 240.degree. ° C and 280 ° C. Generally this increase is less than 60 ° C, preferably less than 50 ° C, more preferably less than 40 ° C.
  • This mode of operation also differs significantly from that of the prior art in which the temperature of the hot flask is set for the operation of the H2S stripper column.
  • the temperature of said separator flask, when it is present, is therefore generally between 280 ° C and 350 ° C, preferably between 300 ° C and 340 ° C and very preferably between 300 ° C and 330 ° C.
  • This rise in temperature is then used to distil a maximum of naphtha in the stripper so as to send to the main fractionation column compounds whose boiling point is generally greater than about 100 ° C.
  • the absence of light compounds in the vacuum column thus makes it possible to obtain complete condensation of the overhead product with a very moderate vacuum (for example 0.1 to 0.5 bar abs).
  • any other method of supplying additional heat other than a furnace may, however, be envisaged in the method according to the invention, in particular those known to those skilled in the art, such as, for example, an additional heat exchanger.
  • the temperature of the vacuum system is generally governed by the condensing temperature of the water coming from the stripping steam of the column.
  • the complete condensation of hydrocarbons and water vapor makes it possible to use a very simple vacuum system that consumes little energy.
  • this process therefore makes it possible to gain most often about 2/3 of the energy consumption of the furnace used in the processes of the prior art. The remaining 1/3 is transferred to the furnace of the reaction loop.
  • Another notable simplification is the preferred possibility of removing the lateral strippers of this column, since the extraction of a large quantity of naphtha in the stripper allows to obtain kerosene and diesel cuts having the correct specification of flash point, generally between 50 and 70 ° C.
  • Figure 1 describes one of the possible embodiments of the method according to the invention. This embodiment is particularly well suited to the case where the conversion of the charge in the hydrodesulphurization reaction section is limited to less than 50% (ie less than 50% by weight of the charge is converted into this section), preferably less than 30%.
  • the feed for example a vacuum gas oil comprising hydrocarbons with boiling points between 370 and 565 ° C
  • the hydrogen preferably in excess of the feed, is fed via line 3 and compressor 4 and then line 5, and mixed with the charge 1 before being admitted into a charge-effluent exchanger (6) via line 2.
  • the exchanger 6 preheats the load by means of the effluent from the hydrodesulphurization reactor 10.
  • the feedstock is fed via line 7 into an oven that makes it possible to reach the temperature level necessary for the hydrodesulfurization reaction, and then the hot feed is sent via the line 9, in the hydrodesulfurization section 10, constituted by at least one hydrodesulfurization reactor comprising at least one hydrodesulphurization catalyst.
  • the effluent from the reactor 10 is then sent to the exchanger 6, then via the line 12 to the separator tank 13.
  • a gaseous fraction is separated in this flask and recovered via the line 14.
  • the desulphurized liquid fraction is recovered in the bottom via line 27.
  • Said gaseous fraction comprises unreacted hydrogen, the hydrogen sulphide (H2S) formed during the reaction, as well as generally light hydrocarbons resulting from the conversion of the hydrocarbons of the charge into the reaction section. hydrodesulfurization.
  • H2S hydrogen sulphide
  • the liquid hydrocarbon phase is recycled via lines 20 and 26 to the liquid effluent from the flask 13 and mixed with this liquid effluent before being sent via line 28 to the stripping column (stripper) 29.
  • the gaseous fraction from the flash tank 19 is sent via line 21 to an amine absorber or a washing column 22 for removing at least a portion of the H 2 S, and then the gaseous fraction containing hydrogen is recycled. via lines 23 and 25 to the hydrodesulphurization reactor, after compression by means of the compressor 24 and mixing with the load 1.
  • the stripper 29 is preferably fed with stripping steam via line 32.
  • a gaseous fraction (generally called acid gas) is recovered via line 30 and via line 31 a naphtha having a final boiling point most often greater than 100 ° C.
  • the liquid recovered at the bottom of the stripper via the line 33 is sent via the fractionation column 34, without it being necessary to reheat it in an oven or exchanger.
  • the fractionation column 34 is operated under vacuum. This is usually a moderate vacuum (for example about 0.25 bar in flash zone). The operation of the column under a moderate vacuum considerably reduces the heat to be supplied to the charge of this column to vaporize the fraction having a boiling point below 370 ° C.
  • the additional heat is preferably provided by an increase in the temperature of the hot separator tank (13) relatively moderate compared to the current practice (for example about 310 ° C instead of 270 ° C).
  • This vacuum column is also fed with stripping steam via line 44.
  • the vacuum separation and maintenance section 37 In the vacuum separation and maintenance section 37, the details of which are not shown because they are known to those skilled in the art, it is possible to separate an aqueous liquid fraction and a hydrocarbon fraction which one does not wish to recover. via line 38.
  • the product obtained line 38 is for example constituted by sections naphtha and / or kerosene and / or gas oil having an initial boiling point greater than 100 ° C.
  • Said section 37 also includes equipment for generating a partial vacuum and maintain it in the column, any equipment known to those skilled in the art can be used, for example an ejector and a condenser or a vacuum pump.
  • the intermediate fraction from the fractionation column via the line 39 is cooled, for example by means of an exchanger (40) and an air condenser (42), and then recovered via the line 43.
  • a gas oil fraction having a final boiling point of less than 370 ° C.
  • the heavy fraction from the fractionation column via the line 45 is also cooled by means of, for example, the exchanger 46 and the aerocondenser 48.
  • the fraction thus obtained via the line 49 is a hydrotreated vacuum gas oil with cooling points. adjacent to the initial charge (eg, initial and final boiling points of 370 ° C and 565 ° C respectively).

Claims (11)

  1. Hydrodesulfurierungsanlage für Gasöl oder Vakuumdestillat umfassend:
    - eine Hydrodesulfurierungssektion, umfassend mindestens einen Hydrodesulfurierungsreaktor,
    - mindestens eine Zuführung (1, 2) in die Hydrodesulfurierungssektion,
    - mindestens eine Gaszuleitung (3, 5, 2) in die Hydrodesulfurierungssektion, wobei das Gas Wasserstoff umfasst,
    - einen Charge-Abstrom-Tauscher (6), der es ermöglicht, die Charge mit Hilfe des Abflusses des Hydrodesulfurierungsreaktors vorzuerhitzen,
    - einen Ofen (8), der sich stromaufwärts zu der Hydrodesulfurierungssektion befindet,
    - mindestens ein Trenngefäß (13), das sich stromabwärts zu der Hydrodesulfurierungssektion befindet und es ermöglicht, den aus der Sektion kommenden Abstrom in eine gasförmige Fraktion (14) und eine entschwefelte flüssige Fraktion (27) zu trennen,
    - mindestens eine Stripkolonne (29), die mit der entschwefelten flüssigen Fraktion (27, 28) und Stripdampf (32) gespeist wird,
    - mindestens eine Fraktionierkolonne (34), die mit der aus der Stripkolonne (32) kommenden flüssigen Fraktion (33) gespeist wird, ohne Anordnung eines Ofens zwischen der Stripsektion und der Fraktioniersektion,
    - mindestens eine Sektion zur Herstellung und Aufrechterhaltung des Vakuums (37).
  2. Anlage nach Anspruch 1, bei der es die Fraktioniersektion ermöglicht, den aus der Stripsektion kommenden flüssigen entschwefelten Abstrom in mindestens 2 Fraktionen zu teilen: eine Fraktion, die vom Schwerbenzin bis zum leichten Gasöl geht, und eine schwere Gasölfraktion.
  3. Anlage nach Anspruch 1, bei der es die Fraktioniersektion ermöglicht, den aus der Stripsektion kommenden flüssigen entschwefelten Abstrom in mindestens 3 Fraktionen zu teilen: eine Fraktion, die vom Schwerbenzin bis zum Kerosin geht und einen Endsiedepunkt zwischen ungefähr 160 °C und ungefähr 180 °C aufweist, eine leichte Gasölfraktion, die einen Endsiedepunkt zwischen ungefähr 350 °C und ungefähr 380 °C aufweist, und eine schwere Gasölfraktion, die einen Anfangssiedepunkt zwischen ungefähr 350 °C und ungefähr 370 °C aufweist.
  4. Anlage nach einem der Ansprüche 1 bis 3, bei der die Reaktionssektion zwei Hydrodesulfurierungsreaktoren in Serie umfasst.
  5. Anlage nach einem der Ansprüche 1 bis 4, ferner umfassend ein Mittel (22) zur Beseitigung mindestens eines Teils des H2S, das in der Hydrodesulfurierungssektion gebildet wird und in der gasförmigen Phase vorhanden ist.
  6. Anlage nach Anspruch 5, bei der das Beseitigungsmittel (22) ein Aminabsorber oder eine Waschsäule ist.
  7. Hydrodesulfurierungsverfahren, das in der Anlage nach einem der Ansprüche 1 bis 6 eingesetzt wird, bei dem das heiße Trenngefäß bei einer Temperatur zwischen 280 °C und 350 °C betrieben wird und die Fraktioniersektion eine Fraktionierkolonne umfasst, die bei einem Druck zwischen 0,05 und 0,95 bar betrieben wird.
  8. Hydrodesulfurierungsverfahren nach Anspruch 7, bei dem das heiße Trenngefäß bei einer Temperatur zwischen 300 °C und 340 °C betrieben wird.
  9. Hydrodesulfurierungsverfahren nach einem der Ansprüche 7 oder 8, bei dem die Fraktioniersektion eine Fraktionierkolonne umfasst, die bei einem Druck zwischen 0,10 und 0,90 bar betrieben wird.
  10. Hydrodesulfurierungsverfahren nach einem der Ansprüche 7 bis 9, bei dem die Hydrodesulfurierungssektion mindestens einen Reaktor umfasst, der mit mindestens einem Hydrodesulfurierungskatalysator beaufschlagt ist.
  11. Verfahren nach Anspruch 10, bei dem der Katalysator mindestens ein Element umfasst, das unter den Elementen der Gruppe VIII und den Elementen der Gruppe VIB des Periodensystems ausgewählt wird.
EP02774912A 2001-10-12 2002-09-09 Verfahren zur hydrodesulfurierung mit einer strippung und einer fraktionierung Expired - Lifetime EP1436362B2 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE60226156T DE60226156T3 (de) 2001-10-12 2002-09-09 Verfahren zur hydrodesulfurierung mit einer strippung und einer fraktionierung

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0113151 2001-10-12
FR0113151A FR2830869B1 (fr) 2001-10-12 2001-10-12 Procede d'hydrodesulfuration comprenant une section de stripage et une section de fractionnement sous vide
PCT/FR2002/003051 WO2003042332A1 (fr) 2001-10-12 2002-09-09 Procede d'hydrodesulfuration comprenant une section de stripage et une section de fractionnement sous vide

Publications (3)

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EP1436362A1 EP1436362A1 (de) 2004-07-14
EP1436362B1 true EP1436362B1 (de) 2008-04-16
EP1436362B2 EP1436362B2 (de) 2011-03-02

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US (1) US7959794B2 (de)
EP (1) EP1436362B2 (de)
AT (1) ATE392460T1 (de)
DE (1) DE60226156T3 (de)
ES (1) ES2305303T5 (de)
FR (1) FR2830869B1 (de)
WO (1) WO2003042332A1 (de)

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CN101250435B (zh) * 2008-03-31 2011-07-20 中国石油化工集团公司 一种烃类加氢转化方法
RU2543719C2 (ru) * 2009-07-15 2015-03-10 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ конверсии углеводородного сырья
US9260672B2 (en) 2010-11-19 2016-02-16 Indian Oil Corporation Limited Process for deep desulfurization of cracked gasoline with minimum octane loss
US20140091010A1 (en) * 2012-09-28 2014-04-03 Uop, Llc Process and apparatus for removing hydrogen sulfide
US9266056B2 (en) * 2013-05-07 2016-02-23 Uop Llc Process for initiating operations of a separation apparatus
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EP1436362A1 (de) 2004-07-14
FR2830869B1 (fr) 2004-07-09
ES2305303T5 (es) 2011-06-24
DE60226156D1 (de) 2008-05-29
ATE392460T1 (de) 2008-05-15
FR2830869A1 (fr) 2003-04-18
DE60226156T2 (de) 2009-07-02
WO2003042332A1 (fr) 2003-05-22
DE60226156T3 (de) 2012-01-26
ES2305303T3 (es) 2008-11-01
EP1436362B2 (de) 2011-03-02
US20050035028A1 (en) 2005-02-17
US7959794B2 (en) 2011-06-14

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