EP1175471A1 - Verfahren zur erzeugung von erdölprodukten mit niedrigem schwefelgehalt durch entschwefelung von extrakten - Google Patents

Verfahren zur erzeugung von erdölprodukten mit niedrigem schwefelgehalt durch entschwefelung von extrakten

Info

Publication number
EP1175471A1
EP1175471A1 EP00925374A EP00925374A EP1175471A1 EP 1175471 A1 EP1175471 A1 EP 1175471A1 EP 00925374 A EP00925374 A EP 00925374A EP 00925374 A EP00925374 A EP 00925374A EP 1175471 A1 EP1175471 A1 EP 1175471A1
Authority
EP
European Patent Office
Prior art keywords
compounds
solvent
diesel
type
sulfur
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.)
Granted
Application number
EP00925374A
Other languages
English (en)
French (fr)
Other versions
EP1175471B1 (de
Inventor
Pedro Da Silva
Rapha[L Le Gall
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
TotalEnergies Marketing Services SA
Original Assignee
Total Raffinage Distribution SA
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Total Raffinage Distribution SA filed Critical Total Raffinage Distribution SA
Publication of EP1175471A1 publication Critical patent/EP1175471A1/de
Application granted granted Critical
Publication of EP1175471B1 publication Critical patent/EP1175471B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
    • C10G53/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
    • 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
    • C10G32/00—Refining of hydrocarbon oils by electric or magnetic means, by irradiation, or by using microorganisms
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/14—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one oxidation step

Definitions

  • the invention relates to a process for obtaining petroleum products which can optionally be used either for the formulation of fuel for an internal combustion engine with compression ignition (of the diesel type), or as fuel, as well as the petroleum product of the diesel type and the by-products obtained by this process.
  • gas oils which are currently on the market in France in the form of fuels for diesel type engines, are products resulting from refining which contain sulfur in an amount at most equal to 0.05% by weight (500 ppm, or parts by million); however, increasingly stringent sulfur content standards are envisaged, in particular by the European Union, for the year 2000 ( ⁇ 350 ppm) and for 2005 ( ⁇ 50 ppm).
  • These gas oils are usually obtained following a so-called hydrosulfurization treatment from very diverse hydrocarbon feedstocks which can come from the direct distillation of crude oil, visbreaking, ydroconversion or catalytic cracking.
  • DBT dibenzothiophenes
  • the catalytic hydrodesulfurization process consumes large quantities of hydrogen and requires operating at increasingly higher temperatures and pressures or at a lower hourly space velocity of the charge, and with more efficient catalysts, when wishes to eliminate these ultimate amounts of sulfur contained in these organosulfur compounds; however this makes the installations more and more expensive and the process less interesting from the economic point of view.
  • the reaction can be stopped at the stage of intermediate products such as hydroxyphenylbenzenesulfinates or their derivatives, which are soluble in water and can therefore be extracted from hydrocarbon feedstocks.
  • intermediate products such as hydroxyphenylbenzenesulfinates or their derivatives, which are soluble in water and can therefore be extracted from hydrocarbon feedstocks.
  • the implementation of such a process requires the formation of an oil / water and biocatalyst emulsion, in a reactor whose volume ratio can be 25/75%, and results in the use of treatment capacities. with high volumes.
  • US Pat. No. 5,232,854 describes a process for advanced desulphurization of a hydrocarbon feed, comprising a conventional hydro-desulphurization step followed by a biocatalytic desulphurization step by incubating the feed in the presence of oxygen with microorganisms such as those described in the patents cited above, and a step of separation of the hydrocarbon effluent having a sulfur content ⁇ 500 ppm, of the residues in the form of non-organic sulfides.
  • a process for advanced desulphurization of a hydrocarbon feed comprising a conventional hydro-desulphurization step followed by a biocatalytic desulphurization step by incubating the feed in the presence of oxygen with microorganisms such as those described in the patents cited above, and a step of separation of the hydrocarbon effluent having a sulfur content ⁇ 500 ppm, of the residues in the form of non-organic sulfides.
  • the aim of the present invention is therefore to improve the advanced desulphurization of hydrocarbon feedstocks with a high sulfur content, without implementing high temperature and pressure conditions, and while developing the by-products obtained. .
  • the Applicant has established that it was particularly judicious to couple extraction and oxidative desulfurization steps, which take place under conditions of low temperature and pressure, close to ambient temperature and atmospheric pressure, and without consumption of hydrogen, therefore very advantageous from an economic point of view, and in particular of concentrating the most refractory organosulfur compounds by an extraction process, then treating the extracts obtained by a process of desulfurization by oxidation, so as to separate the hydrocarbon effluents obtained with a low sulfur content from the oxidized organosulfur compounds and to recover these by-products; these can then be used after treatment, in particular as detergents.
  • the subject of the invention is a process for obtaining petroleum products of the diesel type of improved quality, from a diesel cut containing organosulfur compounds of the dibenzothiophene type and / or their derivatives, with boiling points.
  • initial and final generally between about 170 and 480 ° C, characterized in that it comprises at least two stages, one, a), of liquid / liquid extraction in which the diesel cut is brought into contact with a solvent , so as to obtain a diesel-type raffinate with a low content of sulfur and aromatic compounds and an extract rich in solvent and a high content of sulfur and aromatic compounds, and the other, b), of oxidation of sulfur compounds of l extract, so as to obtain, after separation, a hydrocarbon effluent of the heavy diesel type with low sulfur content, and a residue comprising oxidized organosulfur compounds.
  • the two steps are carried out at pressures less than or equal to 1 MPa, and at temperatures between room temperature and 100 ° C.
  • the solvent used in step a) is chosen from the group consisting of methanol, acetonitrile, monomethylformamide, dimethyl formamide, dimethylacetamide, N-methylpyrolidone, dimethylsulfoxide and furfural.
  • step b) consists of a bio-desulfurization in which the extract, optionally freed of the solvent, preferably at atmospheric pressure, is treated in a reactor, in the presence of a biocatalyst in aqueous phase, comprising an appropriate strain of microorganisms generating enzymes capable of oxidizing organosulfur compounds.
  • step b) when the latter is a bio-desulfurization, is followed by a first step c) of separation of the oily phase containing the hydrocarbon effluent and the aqueous phase, the latter containing the biocatalyst and the residue consisting of organosulfinate type compounds, in particular benzenesulfinates and / or their derivatives; these are formed by the opening of thiophenic cycles by oxidation.
  • the separation of the residue and the biocatalyst is carried out in a second separation step d), which consists either of an extraction with a polar solvent or on ion exchange resins, either by filtration or by adsorption on a solid polar support.
  • step b) consists of chemical oxidation; this can be carried out in particular with oxidizing agents of the peroxide type.
  • the residue from step b), obtained after separation consists of compounds of the sulfoxide or sulfone type.
  • the biodesulfurization step is carried out at pressures below 1 MPa and in particular at atmospheric pressure, in the presence of air, and at temperatures between ambient temperature and 40 ° C.
  • the starting diesel cut is a direct distillation cut, or comes from a drihydrocracking operation, from catalytic, visbreaking or coking cracking; it has a sulfur content generally greater than or equal to 1% by weight.
  • the hydrocarbon effluent from step b) has a final boiling point less than or equal to 380 ° C.
  • the method according to the invention comprises an additional stage of distillation or decantation of the extract from stage a) making it possible to obtain a top product rich in solvent, which is recovered and recycled in stage extraction, and a solvent-depleted bottoms product which is introduced in step b); it is also possible to envisage a stage of distillation of the raffinate from stage a), in order to recover the small quantity of solvent which it still contains.
  • the method also includes an additional step of hydro-treatment of the hydrocarbon effluent obtained in step c), in particular of hydrodesulfurization under mild conditions.
  • a second subject of the invention is the petroleum product of the diesel type obtained by the process according to the invention, having a sulfur content of less than 500 ppm, and preferably less than 50 ppm.
  • a third subject of the invention is the use of the benzenesulfinate type compounds obtained by the process according to the invention, after having subjected them to an additional treatment such as an oxidation followed by an alkylation or alkylation, as hydrotropic agents or surfactants, especially in the manufacture of detergents.
  • step b) The chemical oxidation of step b) can be carried out in homogeneous phase at low temperature (about 70-80 ° C) and at atmospheric pressure, in the presence of a peroxidizing agent (for example hydrogen peroxide) and d 'an acid catalyst such as acetic acid or sulfuric acid.
  • a peroxidizing agent for example hydrogen peroxide
  • d 'an acid catalyst such as acetic acid or sulfuric acid.
  • the separation of the sulfones obtained and the hydrocarbon effluent can be carried out on an adsorbent mass, such as for example silica gel.
  • Any other type of oxidation can be used, and in particular oxidation by oxone (potassium peroxy-monosulfate) is also possible.
  • a first advantage presented by the process according to the invention is that it makes it possible to use hydrocarbon fractions, for example of the diesel type, with an initial boiling point of approximately 170 ° C. and a final boiling point of approximately 375 ° C (the boiling point temperatures indicated are measured according to the TBP "True boiling” distillation method point "), having already undergone conventional catalytic hydrodesulfurization and having a residual sulfur content of less than 500 ppm, and concentrating, by means of the liquid-liquid type extraction step with a solvent having increased selectivity for dibenzothiophenes and their derivatives, these compounds in the extract phase which is sent to the next stage.
  • the raffinate obtained in this extraction consists of a hydrocarbon feedstock with a low content of sulfur and aromatic compounds, which is sent to the engine diesel pool (the pool is the designation designating all the basic products used to make a petroleum product).
  • a second advantage is to carry out the two steps at pressure below 1 MPa and at temperature below 100 ° C, and preferably at atmospheric pressure and at room temperature.
  • LCO type cuts (“Light cycle oil " cut very aroma iu coming from the effluents of a catalytic cracking unit), having much higher sulfur contents, which can reach 2.5% by weight or more.
  • the liquid-liquid extraction step is carried out in a conventional manner, against the current, in an extraction column comprising, as packing, for example fixed disks and rings, rotary disks or static mixers, preferably having 5 at 10 theoretical stages, at a temperature between 30 ° C and 100 ° C, and under a pressure between 0.1 and 1 MPa; the volume ratio of the solvent to the charge is generally from 0.2 / 1 to 5 / 1.
  • the solvent is preferably chosen from the group of solvents making it possible to extract at least part of the mono and polyaromatic and sulfur compounds, this group being made up of methanol, acetonitrile, monomethylformamide, dimethyl formamide, dimethylacetamide, N-methylpyrolidone, dimethylsulfoxide and furfural.
  • a cosolvent which may be a linear or branched alcohol.
  • a raffinate is thus obtained which is a diesel cut with a low sulfur content and which can be sent to the engine diesel pool, after having been purified by elimination of the traces of solvent which it contains, by distillation; moreover, the extract obtained, having a high content of solvent and of sulfur and aromatic compounds, will be sent to step b), after having possibly been sent beforehand to a distillation zone or to any other separation device, in order to recovering a fraction containing almost all of the solvent.
  • Step b) of oxidation of the sulfur compounds is carried out so as to obtain, after separation, a hydrocarbon effluent of the heavy diesel type with reduced sulfur content, which can be sent to the domestic fuel pool, and a residue comprising compounds oxidized organosulfur.
  • step b) is a bio-desulfurization
  • the efficiency of the desulphurization depends on the nature of the feed and that it decreases according to whether the diesel is obtained by coking, by visbreaking, by catalytic cracking (LCO). ) and by direct distillation (GOSR, "GAZ Oil Straight Run).
  • the hydrocarbon fraction used comes from an A.rabc Light diesel oil for direct distillation, after fractionation and at an initial distillation point of 320 ° C. and a final distillation point of 380 ° C, a density at 15 "C of 0.87, a polyaromatic content of 14% by weight and a sulfur content of 1.8% by weight; it is introduced via line 1 into the liquid-liquid extraction column 2, operating at atmospheric pressure and at a temperature of 80 ° C., into which is introduced via line 3 an identical volume amount of counter-current furfural.
  • a diesel-type raffinate is obtained, having a sulfur content of 0.8% by weight, which after having been freed from the solvent by distillation, is sent via line 4 to a hydrodesulfurization reactor 5, operating under usual conditions such as a partial hydrogen pressure of 2.5 MPa, a temperature of 340 ° C, an hourly space velocity (WH) of 1.1 h 1 , a ratio of the flow of hydrogen to the load of 125 Nl / 1 (NI being "Normal" liters), in the presence of a cobalt-molybdenum catalyst supported on alumina, so as to obtain an effluent having a sulfur content of 29 ppm and a density of 0.825, sent via line 20 to the pool diesel fuel and which meets the specifications planned for 2005; an extract having a sulfur content of 5% by weight is recovered via line 6, which, after having been freed in a distillation column 7, of the solvent which is recycled via line 8 to the extraction column 2, is sent via line 9 to the bio-desulfurization reactor 10, operating in the presence
  • reaction products from line 12 are introduced into a separator 13 from which line 14 is recovered a hydrocarbon effluent of the heavy diesel type, containing 1% by weight of sulfur, which to be sent to the pool domestic fuel oil (sulfur content ⁇ 0.2%), must undergo hydrodesulfurization under conditions similar to those prevailing in reactor 5 (for example at a temperature between 330 and 340 ° C.) so as to obtain a content of 0, 17% by weight of sulfur.
  • the hydrocarbon fraction used comes from a light Arabic diesel fuel for distillation direct, has an initial distillation point of 180 ° C and an end distillation point of 380 ° C, and has undergone a hydrodesulfurization treatment so as to have a sulfur content of 200 ppm; this cut undergoes fractionation allowing to obtain a top product which is a cut whose final boiling point is less than 328 ° C and has a sulfur content of 40 ppm, therefore satisfies the specification planned in 2005 for diesel fuel, and a bottoms product whose initial boiling point is greater than 328 ° C (cut 328-380 ° C), containing sulfur compounds in high concentration and having a sulfur content of 720 ppm, which is sent to the next extraction step.

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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)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Crystals, And After-Treatments Of Crystals (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP00925374A 1999-05-05 2000-05-03 Verfahren zur erzeugung von erdölprodukten mit niedrigem schwefelgehalt durch entschwefelung von extrakten Expired - Lifetime EP1175471B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR9905700A FR2793256B1 (fr) 1999-05-05 1999-05-05 Procede d'obtention de produits petroliers a faible taux de soufre par desulfuration d'extraits
FR9905700 1999-05-05
PCT/FR2000/001188 WO2000068342A1 (fr) 1999-05-05 2000-05-03 Procede d'obtention de produits petroliers a faible taux de soufre par desulfuration d'extraits

Publications (2)

Publication Number Publication Date
EP1175471A1 true EP1175471A1 (de) 2002-01-30
EP1175471B1 EP1175471B1 (de) 2002-12-04

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP00925374A Expired - Lifetime EP1175471B1 (de) 1999-05-05 2000-05-03 Verfahren zur erzeugung von erdölprodukten mit niedrigem schwefelgehalt durch entschwefelung von extrakten

Country Status (8)

Country Link
US (1) US6638419B1 (de)
EP (1) EP1175471B1 (de)
AT (1) ATE229063T1 (de)
DE (1) DE60000934T2 (de)
ES (1) ES2187468T3 (de)
FR (1) FR2793256B1 (de)
PT (1) PT1175471E (de)
WO (1) WO2000068342A1 (de)

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US8221706B2 (en) * 2009-06-30 2012-07-17 Uop Llc Apparatus for multi-staged hydroprocessing
US8518241B2 (en) * 2009-06-30 2013-08-27 Uop Llc Method for multi-staged hydroprocessing
US20110000823A1 (en) * 2009-07-01 2011-01-06 Feras Hamad Membrane desulfurization of liquid hydrocarbons using an extractive liquid membrane contactor system and method
RU2441055C2 (ru) * 2010-04-21 2012-01-27 Федеральное государственное образовательное учреждение высшего профессионального образования Астраханский государственный технический университет (ФГОУ ВПО АГТУ) Способ получения экологически чистого дизельного топлива
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Also Published As

Publication number Publication date
DE60000934T2 (de) 2003-05-08
DE60000934D1 (de) 2003-01-16
FR2793256B1 (fr) 2001-07-27
WO2000068342A1 (fr) 2000-11-16
ES2187468T3 (es) 2003-06-16
US6638419B1 (en) 2003-10-28
PT1175471E (pt) 2003-03-31
ATE229063T1 (de) 2002-12-15
FR2793256A1 (fr) 2000-11-10
EP1175471B1 (de) 2002-12-04

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