EP0583836A1 - Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen - Google Patents

Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen Download PDF

Info

Publication number
EP0583836A1
EP0583836A1 EP93202395A EP93202395A EP0583836A1 EP 0583836 A1 EP0583836 A1 EP 0583836A1 EP 93202395 A EP93202395 A EP 93202395A EP 93202395 A EP93202395 A EP 93202395A EP 0583836 A1 EP0583836 A1 EP 0583836A1
Authority
EP
European Patent Office
Prior art keywords
process according
hydrocarbon
catalyst
hydrogen
hydroconversion
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
EP93202395A
Other languages
English (en)
French (fr)
Other versions
EP0583836B1 (de
EP0583836B2 (de
Inventor
Jacobus Eilers
Sytze Abel Posthuma
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=8210862&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0583836(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to EP93202395A priority Critical patent/EP0583836B2/de
Publication of EP0583836A1 publication Critical patent/EP0583836A1/de
Publication of EP0583836B1 publication Critical patent/EP0583836B1/de
Application granted granted Critical
Publication of EP0583836B2 publication Critical patent/EP0583836B2/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with 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
    • 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
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps

Definitions

  • the present invention relates to a process for the preparation of hydrocarbons suitable for use as fuels, in particular to a process for the preparation of such hydrocarbons from a mixture of carbon monoxide and hydrogen.
  • the preparation of hydrocarbons from a mixture comprising carbon monoxide and hydrogen by contacting the mixture with a suitable synthesis catalyst at elevated temperatures and pressures is known in the art as the Fischer-Tropsch synthesis. It is known in the art to apply Fischer-Tropsch synthesis processes in the preparation of a range of principly aliphatic hydrocarbons having a wide range of molecular weights. Of particular interest, however, is the use of the Fischer-Tropsch synthesis to prepare hydrocarbons suitable for use as fuels, for example hydrocarbons having boiling points within the boiling point ranges of naphtha and the middle distillates.
  • mishtha is a reference to hydrocarbons or hydrocarbon mixtures having a boiling point or boiling point range substantially corresponding to that of the naphtha (sometimes referred to as the gasoline) fractions obtained during the conventional atmospheric distillation of crude oil.
  • the following fractions are consecutively recovered from the crude oil: one or more naphtha fractions boiling in the range of from 30 to 220 °C, one or more kerosine fractions boiling in the range of from 120 to 300 °C and one or more gasoil fractions boiling in the range of from 170 to 370 °C.
  • hydrocarbon fuel is to be taken as a reference to either one of or a mixture of naphtha and middle distillates.
  • US-A-4,478,955 discloses a process scheme comprising contacting the effluent of a Fischer-Tropsch synthesis process with hydrogen in the presence of a suitable hydrogenation catalyst.
  • the effluent of the Fischer-Tropsch synthesis is described in US-A-4,478,955 as comprising predominantly olefins and carboxylic acids.
  • useful fuel components comprising alkanes, alcohols and esters are produced.
  • the present invention provides a process for the preparation of hydrocarbon fuels comprising the steps of:
  • the products of the hydrocarbon synthesis stage are subjected to a hydroconversion treatment.
  • the primary objective of the hydroconversion is to convert, by hydrocracking, the high molecular weight, paraffinic products of the synthesis stage into the desired hydrocarbon fuels, for example middle distillates.
  • the hydroconversion treatment serves to isomerise a portion of the linear paraffinic hydrocarbons, which in turn improves the properties of the hydrocarbon fuels.
  • the action of the hydroconversion treatment is to hydrogenate the minor quantities of olefinic and oxygen-containing compounds formed during the hydrocarbon synthesis reactions and which are undesirable components in hydrocarbon fuels.
  • the hydrocarbons prepared in the first stage, stage (a), of the process of the present invention are subjected to a hydroconversion in two separate and distinct stages.
  • the olefinic and oxygen-containing compounds are hydrogenated.
  • the operating conditions of the first hydroconversion stage are selected so as to substantially prevent hydrocracking and/or hydroisomerisation reactions from occurring.
  • stage (c) the desired hydrocarbon fuels are prepared by subjecting at least a part of the product of the first hydroconversion stage to a second hydroconversion treatment, in which the high molecular weight paraffinic hydrocarbons are hydroisomerised and hydrocracked.
  • water is formed as a product of the hydrogenation of the oxygen-containing hydrocarbons. It has been found that water produced during this reaction adversely affects certain hydroconversion catalysts, leading to a reduction in catalyst performance.
  • milder operating conditions are required in the second hydroconversion stage to achieve the desired degree of hydrocracking and hydroisomerisation than required in the single hydroconversion stage of the prior art process. This results in a improved lifetime of the hydroconversion catalyst and, most surprisingly, leads to a markedly improved product.
  • the process of the present invention most surprisingly exhibits an improved selectivity to valuable hydrocarbon fuels, in particular gasoil, compared with the processes of the prior art.
  • substantially paraffinic when used in connection with hydrocarbon products or hydrocarbon fuels refers to a hydrocarbon mixture comprising at least 70 %wt paraffins, preferably at least 80 %wt paraffins.
  • Hydrocarbon fuels produced by the process of this invention typically comprise at least 90 %wt paraffins, more typically at least 95 %wt paraffins.
  • a feed comprising a mixture of carbon monoxide and hydrogen is contacted at elevated temperature and pressure with a catalyst active in the synthesis of paraffinic hydrocarbons.
  • Suitable processes for the preparation of the mixture of carbon monoxide and hydrogen are well known in the art and include such processes as the partial oxidation of methane, typically in the form of natural gas, and the steam reforming of methane.
  • the relative amounts of carbon monoxide and hydrogen present in the feed may vary over a wide range and may be selected according to the precise catalyst and process operating conditions being employed.
  • the feed contacting the catalyst comprises carbon monoxide and hydrogen in a hydrogen/carbon monoxide molar ratio of below 2.5, preferably below 1.75. More preferably, the hydrogen/carbon monoxide ratio is in the range of from 0.4 to 1.5, especially from 0.9 to 1.3.
  • Unconverted carbon monoxide and hydrogen may be separated from the synthesis product and recycled to the inlet of the synthesis reactor.
  • the catalyst comprises, as the catalytically active component, a metal from Group VIII of the Periodic Table of Elements.
  • a metal from Group VIII include ruthenium, iron, cobalt and nickel.
  • a catalyst comprising cobalt as the catalytically active metal is preferred.
  • the catalytically active metal is preferably supported on a porous carrier.
  • the porous carrier may be selected from any suitable refractory metal oxide or silicate or mixture thereof. Particular examples of preferred carriers include silica, alumina, titania, zirconia and mixtures thereof. Carriers comprising silica and/or alumina are especially preferred.
  • the catalytically active metal may be applied to the carrier by any of the techniques known in the art, for example comulling, impregnation or precipitation. Impregnation is a particularly preferred technique, in which the carrier is contacted with a compound of the catalytically active metal in the presence of a liquid, most conveniently in the form of a solution of the metal compound.
  • the compound of the active metal may be inorganic or organic, with inorganic compounds being preferred, in particular nitrates.
  • the liquid employed may also be either organic or inorganic. Water is a most convenient liquid.
  • the amount of catalytically active metal present on the carrier is typically in the range of from 1 to 100 parts by weight, preferably 10 to 50 parts by weight, per 100 parts by weight of carrier material.
  • the catalytically active metal may be present in the catalyst together with one or more metal promoters or co-catalysts.
  • the promoters may be present as metals or as the metal oxide, depending upon the particular promoter concerned. Suitable metal oxide promoters include oxides of metals from Groups IIA, IIIB, IVB, VB or VIB of the Periodic Table, oxides of the lanthanides and/or the actinides.
  • the catalyst comprises an oxide of an element in Group IVB of the Periodic Table, in particular titanium or zirconium. Catalysts comprising zirconium are especially preferred.
  • the catalyst may comprise a metal promoter selected from Groups VIIB and/or VIII of the Periodic Table.
  • Preferred metal promoters include platinum and palladium.
  • a most suitable catalyst comprises cobalt as the catalytically active metal and zirconium as a promoter.
  • the promoter may be incorporated in the catalyst using any of the methods discussed hereinbefore with respect to the catalytically active component.
  • the promoter if present in the catalyst, is typically present in an amount of from 1 to 60 parts by weight, preferably from 2 to 40 parts by weight, per 100 parts by weight of carrier material.
  • the hydrocarbon synthesis is conducted under conditions of elevated temperature and pressure. Typically, the synthesis is effected at a temperature in the range of from 125 to 300 °C, preferably from 175 to 250 °C.
  • the reaction pressure is typically in the range of from 5 to 100 bar, preferably from 12 to 50 bar.
  • the synthesis may be conducted using a variety of reactor types and reaction regimes, for example in a fixed bed regime, a slurry phase regime or an ebullating bed regime.
  • the hydrocarbon product of the synthesis stage is subjected to a two-stage hydroconversion treatment in stages (b) and (c) of the process of the present invention.
  • the entire effluent of the synthesis stage may be led directly to the first hydroconversion stage.
  • the low molecular weight products of the synthesis stage in particular the C4- fraction, for example methane, ethane and propane, may also be removed prior to the hydroconversion treatment.
  • the separation is conveniently effected using distillation techniques well known in the art.
  • the hydrocarbon product is contacted with hydrogen in the presence of a hydrogenation catalyst.
  • a hydrogenation catalyst Suitable catalysts for use in this stage are known in the art.
  • the catalyst comprises as catalytically active component one or more metals selected from Groups VIB and VIII of the Periodic Table of Elements, in particular one or more metals selected from molybdenum, tungsten, cobalt, nickel, ruthenium, iridium, osmium, platinum and palladium.
  • the catalyst comprises on or more metals selected from nickel, platinum and palladium as the catalytically active component.
  • a particularly suitable catalyst comprises nickel as a catalytically active component.
  • Catalysts for use in the first hydroconversion stage typically comprise a refractory metal oxide or silicate as a carrier.
  • Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania and mixtures thereof.
  • Preferred carrier materials for inclusion in the catalyst for use in the process of this invention are silica, alumina and silica-alumina.
  • the catalyst may comprise the catalytically active component in an amount of from 0.05 to 80 parts by weight, preferably from 0.1 to 70 parts by weight, per 100 parts by weight of carrier material.
  • the amount of catalytically active metal present in the catalyst will vary according to the specific metal concerned.
  • One particularly suitable catalyst for use in the first hydroconversion stage comprises nickel in an amount in the range of from 30 to 70 parts by weight per 100 parts by weight of carrier material.
  • a second particularly suitable catalyst comprises platinum in an amount in the range of from 0.05 to 2.0 parts by weight per 100 parts by weight of carrier material.
  • Suitable catalysts for use in the first hydroconversion stage of the process of this invention are available commercially, or may be prepared by methods well known in the art, for example the methods discussed hereinbefore with reference to the preparation of the hydrocarbon synthesis catalyst.
  • the hydrocarbon product is contacted with hydrogen at elevated temperature and pressure.
  • the operating temperature may typically range from 100 to 300 °C, more preferably from 150 to 275 °C, in particular from 175 to 250 °C.
  • the operating pressure ranges from 5 to 150 bars, preferably from 10 to 50 bars.
  • Hydrogen may be supplied to the hydroconversion stage at a gas hourly space velocity in the range of from 100 to 10000 Nl/l/hr, more preferably from 250 to 5000 Nl/l/hr.
  • the hydrocarbon product being treated is typically supplied to the hydroconversion stage at a weight hourly space velocity in the range of from 0.1 to 5 kg/l/hr, more preferably from 0.25 to 2.5 kg/l/hr.
  • the ratio of hydrogen to hydrocarbon product may range from 100 to 5000 Nl/kg and is preferably from 250 to 3000 Nl/kg.
  • the first hydroconversion stage is operated under conditions such that substantially no isomerisation or hydrocracking of the feed occurs.
  • the precise operating conditions required to achieve the desired degree of hydrogenation without substantial hydrocracking or hydroisomerisation occurring will vary according to the composition of the hydrocarbon product being fed to the hydroconversion stage and the particular catalyst being employed.
  • the degree of conversion of the feed hydrocarbon may be determined. In this respect, conversion, in percent, is defined as the percent weight of the fraction of the feed boiling above 370 °C which is converted during the hydroconversion to a fraction boiling below 370 °C.
  • the conversion of the first hydroconversion stage is below 20%, preferably below 10%, more preferably below 5%.
  • the hydrocarbon product leaving the first hydroconversion stage substantially consists of high molecular weight, paraffinic hydrocarbons having a boiling point range above that of the middle distillates. At least a part of this hydrocarbon product is subjected to a second hydroconversion in stage (c) of the process of this invention, to yield the desired hydrocarbon fuel product. If desired, the entire effluent of the first hydroconversion stage may be led directly to the second hydroconversion stage. However, it is preferred to separate the low molecular weight hydrocarbons, especially the C4-fraction, from the higher molecular weight hydrocarbons prior to the second hydroconversion stage. The separation may be conveniently achieved using distillation techniques well known in the art. At least a part of the remaining C5+ fraction of the hydrocarbon product is then used as feed for the second hydroconversion stage.
  • the catalyst comprises as catalytically active component one or more metals selected from Groups VIB and VIII of the Periodic Table of Elements, in particular one or more metals selected from molybdenum, tungsten, cobalt, nickel, ruthenium, iridium, osmium, platinum and palladium.
  • the catalyst comprises one or more metals selected from nickel, platinum and palladium as the catalytically active component. Catalysts comprising platinum as the catalytically active component have been found to be particularly suitable for use in the second hydroconversion stage.
  • Catalysts for use in the second hydroconversion stage typically comprise a refractory metal oxide or silicate as a carrier.
  • the carrier material may be amorphous or crystalline. Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania and mixtures thereof.
  • the carrier may comprise one or more zeolites, either alone or in combination with one or more of the aforementioned carrier materials.
  • Preferred carrier materials for inclusion in the catalyst for use in the process of this invention are silica, alumina and silica-alumina.
  • a particularly preferred catalyst comprises platinum supported on a silica-alumina carrier.
  • the catalyst may comprise the catalytically active component in an amount of from 0.05 to 80 parts by weight, preferably from 0.1 to 70 parts by weight, per 100 parts by weight of carrier material.
  • the amount of catalytically active metal present in the catalyst will vary according to the specific metal concerned.
  • a particularly preferred catalyst for use in the second hydroconversion stage comprises platinum in an amount in the range of from 0.05 to 2 parts by weight, more preferably from 0.1 to 1 parts by weight, per 100 parts by weight of carrier material.
  • Suitable catalysts for use in the second hydroconversion stage of the process of this invention are available commercially, or may be prepared by methods well known in the art, for example the methods discussed hereinbefore with reference to the preparation of the hydrocarbon synthesis catalyst.
  • the hydrocarbon product of the first hydroconversion stage is contacted with hydrogen in the presence of the catalyst at elevated temperature and pressure.
  • the temperatures necessary to yield the hydrocarbon fuels will lie in the range of from 175 to 400 °C, preferably from 250 to 375 °C.
  • the pressure typically applied ranges from 10 to 250 bars, more preferably from 25 to 250 bars.
  • Hydrogen may be supplied at a gas hourly space velocity of from 100 to 10000 Nl/l/hr, preferably from 500 to 5000 Nl/l/hr.
  • the hydrocarbon feed may be provided at a weight hourly space velocity of from 0.1 to 5 kg/l/hr, preferably from 0.25 to 2 kg/l/hr.
  • the ratio of hydrogen to hydrocarbon feed may range from 100 to 5000 Nl/kg and is preferably from 250 to 2500 Nl/kg.
  • the degree of hydrocracking and isomerisation occurring in the second hydroconversion stage may be measured by determining the degree of conversion of the fraction boiling above 370 °C, as hereinbefore defined.
  • the second hydroconversion stage is operated at a conversion of at least 40%.
  • the hydrogen required for the operation of both the first and the second hydroconversion stages may be generated by processes well known in the art, for example by the steam reforming of a refinery fuel gas.
  • the hydrocarbon fuel produced in the second hydroconversion stage will typically comprise hydrocarbons having boiling points lying in a number of different fuel fractions, for example the naphtha, kerosine and gasoil fractions discussed hereinbefore. Separation of the hydrocarbon fuel into the appropriate fractions may be conveniently achieved using distillation techniques well known in the art.
  • Polyelectrolyte (Nalco; as a 4% aqueous solution) was added and the resulting mixture mulled for a further 5 minutes to yield a final mixture having a pH of about 8.4 and a loss on ignition of about 70%.
  • the resulting mixture was extruded using a 1" Bonnot extruder having a 1.7 mm Delrin trilobe dieplate insert to yield trilobe extrudates.
  • the extrudates were dried at a temperature of about 120 °C and finally calcined at a temperature between 500 and 550 °C for 2 hours.
  • the calcined extrudates were washed using an aqueous solution of ammonium acetate and thereafter calcined as hereinbefore described.
  • An aqueous solution was prepared by dissolving cobalt nitrate (Co(NO3)2.6H2O; sufficient to yield an 18% aqueous solution) in water and heated to a temperature of 80 °C.
  • the extrudates were impregnated by immersion in the cobalt nitrate solution for a period of 8 hours at 80 °C.
  • the thus impregnated extrudates were dried and finally calcined at a temperature of 500 °C for from 1 to 2 hours.
  • the catalyst prepared in (i) hereabove was loaded into a reaction vessel.
  • the catalyst was first activated by reduction by being contacted with a mixture of hydrogen and nitrogen at a temperature of 250 °C, a pressure of 5 bar and a gas hourly space velocity of from 500 to 600 Nl/l/hr.
  • the activated catalyst was then contacted with a mixture of carbon monoxide and hydrogen having a hydrogen/carbon monoxide ratio of 1.1 at a gas inlet pressure of from 35 to 40 bars and a gas hourly space velocity of from 1000 to 1200 Nl/l/hr.
  • a heavy wax was produced.
  • a mixture comprising amorphous silica-alumina (ex Grace Davison, pore volume (H2O) 1.10 ml/g, 13 %wt alumina (dry basis)), and alumina (ex Criterion Catalyst Co.) was placed in a mulling machine and mulled for a period of about 10 minutes.
  • Acetic acid (10 %wt solution) and water were added and the resulting mixture mulled for a further 10 minutes.
  • polyacrylamide Superfloc A1839, 2 %wt aqueous solution
  • polyelectrolyte Naalco, 4 %wt aqueous solution
  • the resulting mixture was extruded using a 2.25" Bonnot extruder through a dieplate, yielding 2.5 mm trilobe extrudates.
  • the resulting extrudates were dried at a temperature of 120 °C for about 2 hours and subsequently calcined at a temperature of 600 °C for 2 hours.
  • aqueous solution comprising hexachloroplatinic acid (H2PtCl6, 2.45 %wt) and nitric acid (7.66 %wt) having a pH of below 1.
  • H2PtCl6, 2.45 %wt hexachloroplatinic acid
  • nitric acid 7.66 %wt
  • the extrudates were impregnated using this aqueous solution via the Pore Impregnation technique to give a final platinum loading on the carrier of 0.8 %wt.
  • the thus impregnated extrudates were finally calcined at a temperature of 500 °C for about 2 hours.
  • the catalyst prepared in (i) hereabove was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the hydrocarbon synthesis stage was fed to the reaction vessel at a weight hourly space velocity of 0.88 kg/l/hr, a temperature of 315 °C and a pressure of 35 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 660 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 750 Nl/kg).
  • the conversion achieved in terms of percent weight of the fraction of the feed having a boiling point above 370 °C converted to products having a boiling point of below 370 °C, was 16%, indicating that substantially no cracking or isomerisation of the feed hydrocarbon occurred.
  • a catalyst was prepared following the procedure described in Example 1(B)(i) hereabove.
  • the catalyst prepared in (i) was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the first hydroconversion stage was fed to the reaction vessel at a weight hourly space velocity of 1.046 kg/l/hr and a pressure of 31 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 660 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 630 Nl/kg).
  • a liquid recycle rate of 0.17 kg/l/hr was applied.
  • a conversion target of 55% (as defined in Example 1(B) (ii) hereabove) was set and was achieved by adjusting the operating temperature of the second hydroconversion stage. It was found that an operating temperature of 330 °C was required.
  • the effluent of the reaction vessel was collected and separated by means of distillation into a number of fractions.
  • the properties of a gasoil fraction boiling in the temperature range of from 170 to 340 °C recovered from the effluent are given in Table 1.
  • Example 1(C)(i) hereabove A sample of the catalyst prepared as described in Example 1(C)(i) hereabove was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the hydrocarbon synthesis stage was fed to the reaction vessel at a weight hourly space velocity of 1.103 kg/l/hr and a pressure of 31 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 660 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 596 Nl/kg).
  • a liquid recycle rate of 0.23 kg/l/hr was applied.
  • a conversion of 55% (as defined in Example 1(B) (ii) hereabove) was achieved at an operating temperature of 338 °C.
  • the effluent of the reaction vessel was collected and separated by means of distillation into a number of fractions.
  • the properties of a gasoil fraction boiling in the temperature range of from 170 to 340 °C recovered from the effluent are given in Table 1.
  • Example 1(C)(i) hereabove A sample of the catalyst prepared as described in Example 1(C)(i) hereabove was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the hydrocarbon synthesis stage was fed to the reaction vessel at a weight hourly space velocity of 1.01 kg/l/hr and a pressure of 31.4 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 660 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 655 Nl/kg).
  • a liquid recycle rate of 0.13 kg/l/hr was applied.
  • a conversion of 39% (as defined in Example 1(B) (ii) hereabove) was achieved at an operating temperature of 334 °C.
  • the effluent of the reaction vessel was collected and separated by means of distillation into a number of fractions.
  • the properties of a gasoil fraction boiling in the temperature range of from 160 to 340 °C recovered from the effluent are given in Table 1.
  • a catalyst was prepared using the general method outlined in Example 1(A)(i) hereabove and used to prepare a C5+ hydrocarbon product following the general procedure described in Example 1(A) (ii) hereabove.
  • a commercially available nickel-containing hydrogenation catalyst (60 %wt nickel; ex Harshaw Catalysts) was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the hydrocarbon synthesis stage was fed to the reaction vessel at a weight hourly space velocity of 1.0 kg/l/hr, a temperature of 220 °C and a pressure of 30 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 1000 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 1000 Nl/kg).
  • a catalyst was prepared following the procedure described in Example 1(B)(i) hereabove.
  • the catalyst prepared in (i) was loaded into a reaction vessel.
  • the C5+ hydrocarbon product of the first hydroconversion stage was fed to the reaction vessel at a weight hourly space velocity of 1.25 kg/l/hr and a pressure of 30 bars.
  • Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 1000 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 800 Nl/kg).
  • a conversion target of 60% (as defined in Example 4(B) hereabove) was set and achieved by adjusting the operating temperature of the second hydroconversion stage. It was found that an operating temperature of 334 °C was required.
  • the effluent of the reaction vessel was collected and separated by means of distillation into a number of fractions.
  • the selectivity of the second hydroconversion stage to a gasoil fraction boiling in the temperature range of from 220 to 370 °C was 50%.
  • Example 4(A) hereabove product from the hydrocarbon synthesis stage as described in Example 4(A) hereabove was treated to a single hydroconversion stage, operated to yield hydrocarbon fuels, as follows: Catalyst prepared as described in Example 1(B)(i) was loaded into a reaction vessel. The C5+ hydrocarbon product of the hydrocarbon synthesis stage was fed to the reaction vessel at a weight hourly space velocity of 1.25 kg/l/hr and a pressure of 30 bars. Hydrogen was supplied to the reaction vessel at a gas hourly space velocity of 1000 Nl/l/hr (that is a hydrogen to hydrocarbon ratio of 800 Nl/kg). A conversion target of 60% (as defined in Example 4(B) hereabove) was set and achieved by adjusting the operating temperature of the second hydroconversion stage. It was found that an operating temperature of 338 °C was required.
  • the effluent of the reaction vessel was collected and separated by means of distillation into a number of fractions.
  • the selectivity of the second hydroconversion stage to a gasoil fraction boiling in the temperature range of from 220 to 370 °C was 40%.

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)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Liquid Carbonaceous Fuels (AREA)
EP93202395A 1992-08-18 1993-08-16 Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen Expired - Lifetime EP0583836B2 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP93202395A EP0583836B2 (de) 1992-08-18 1993-08-16 Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP92202537 1992-08-18
EP92202537 1992-08-18
EP93202395A EP0583836B2 (de) 1992-08-18 1993-08-16 Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen

Publications (3)

Publication Number Publication Date
EP0583836A1 true EP0583836A1 (de) 1994-02-23
EP0583836B1 EP0583836B1 (de) 1997-10-29
EP0583836B2 EP0583836B2 (de) 2002-02-13

Family

ID=8210862

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93202395A Expired - Lifetime EP0583836B2 (de) 1992-08-18 1993-08-16 Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen

Country Status (13)

Country Link
EP (1) EP0583836B2 (de)
JP (1) JP3522797B2 (de)
AU (1) AU666960B2 (de)
CA (1) CA2104158C (de)
DE (1) DE69314879T3 (de)
DK (1) DK0583836T4 (de)
DZ (1) DZ1708A1 (de)
ES (1) ES2110051T5 (de)
MY (1) MY108862A (de)
NO (1) NO305288B1 (de)
NZ (1) NZ248415A (de)
RU (1) RU2101324C1 (de)
ZA (1) ZA935964B (de)

Cited By (117)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0668342A1 (de) * 1994-02-08 1995-08-23 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung von Basisschmieröl
WO1999041217A1 (en) * 1998-02-13 1999-08-19 Exxon Research And Engineering Company Gas conversion using synthesis gas produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
US6121333A (en) * 1998-06-25 2000-09-19 Agip Petroli S.P.A. Process for the preparation of hydrocarbons from synthesis gas
EP1088879A1 (de) * 1999-09-30 2001-04-04 Institut Francais Du Petrole Verfahren zur Erzeugung von Benzin mit verbesserter Oktanzahl
GB2369370A (en) * 2000-10-23 2002-05-29 Chevron Usa Inc Addition of hydrogen to hydrocarbon streams to prevent fouling
US6497812B1 (en) 1999-12-22 2002-12-24 Chevron U.S.A. Inc. Conversion of C1-C3 alkanes and fischer-tropsch products to normal alpha olefins and other liquid hydrocarbons
US6515032B2 (en) 2001-05-11 2003-02-04 Chevron U.S.A. Inc. Co-hydroprocessing of fischer-tropsch products and natural gas well condensate
SG94676A1 (en) * 1994-02-08 2003-03-18 Shell Int Research Lubricating base oil preparation process
US6544407B1 (en) * 1999-11-19 2003-04-08 Agip Petroli S.P.A. Process for the preparation of middle distillates starting from linear paraffins
US6635171B2 (en) 2001-01-11 2003-10-21 Chevron U.S.A. Inc. Process for upgrading of Fischer-Tropsch products
US6709569B2 (en) 2001-12-21 2004-03-23 Chevron U.S.A. Inc. Methods for pre-conditioning fischer-tropsch light products preceding upgrading
WO2004074406A1 (en) * 2003-02-18 2004-09-02 Chevron U.S.A. Inc. Process for producing premium fischer-tropsch diesel and lube base oils
EP1272592B1 (de) * 2000-04-04 2004-09-29 ExxonMobil Research and Engineering Company Verfahren zum einstellen der härte von fischer-tropschwachs durch mischung
US6858127B2 (en) 2001-03-05 2005-02-22 Shell Oil Company Process for the preparation of middle distillates
GB2386904B (en) * 2002-01-31 2005-02-23 Chevron Usa Inc Upgrading fischer-tropsch and petroleum-derived naphthas and distillates
US6863802B2 (en) 2002-01-31 2005-03-08 Chevron U.S.A. Upgrading fischer-Tropsch and petroleum-derived naphthas and distillates
WO2005026297A1 (en) 2003-09-17 2005-03-24 Shell Internationale Research Maatschappij B.V. Petroleum- and fischer-tropsch- derived kerosene blend
US6939999B2 (en) 2003-02-24 2005-09-06 Syntroleum Corporation Integrated Fischer-Tropsch process with improved alcohol processing capability
US6982355B2 (en) 2003-08-25 2006-01-03 Syntroleum Corporation Integrated Fischer-Tropsch process for production of linear and branched alcohols and olefins
WO2006010068A1 (en) * 2004-07-08 2006-01-26 Conocophillips Company Synthetic hydrocarbon products
US7033552B2 (en) 2002-01-31 2006-04-25 Chevron U.S.A. Inc. Upgrading Fischer-Tropsch and petroleum-derived naphthas and distillates
US7151163B2 (en) 2003-04-28 2006-12-19 Sequoia Pharmaceuticals, Inc. Antiviral agents for the treatment, control and prevention of infections by coronaviruses
US7156978B2 (en) * 2001-07-06 2007-01-02 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking of two fractions from feeds originating from the fischer-tropsch process
FR2888584A1 (fr) * 2005-07-18 2007-01-19 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage de charges issues du procede fischer-tropsch utilisant un lit de garde multifonctionnel
WO2007009987A1 (en) * 2005-07-20 2007-01-25 Shell Internationale Research Maatschappij B.V. Hydrocarbon synthesis process
US7189269B2 (en) 2002-10-18 2007-03-13 Shell Oil Company Fuel composition comprising a base fuel, a fischer tropsch derived gas oil, and an oxygenate
US7220349B2 (en) 2001-07-06 2007-05-22 Institut Francais Du Petrole Process for the production of middle distillates by two-step hydroisomerisation and hydrocracking of feeds from the Fischer-Tropsch process
US7229481B2 (en) 2002-11-13 2007-06-12 Shell Oil Company Diesel fuel compositions
US7326331B2 (en) * 2001-07-06 2008-02-05 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the fischer-tropsch process
US7345211B2 (en) 2004-07-08 2008-03-18 Conocophillips Company Synthetic hydrocarbon products
US7354507B2 (en) 2004-03-17 2008-04-08 Conocophillips Company Hydroprocessing methods and apparatus for use in the preparation of liquid hydrocarbons
US7404890B2 (en) 2001-07-06 2008-07-29 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the Fischer-Tropsch process
FR2917419A1 (fr) * 2007-06-12 2008-12-19 Inst Francais Du Petrole Procede de production de distilltats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
CN101410490A (zh) * 2006-03-31 2009-04-15 新日本石油株式会社 蜡的加氢裂化方法和燃料基材的制造方法
EP1268712B2 (de) † 2000-04-04 2009-06-10 ExxonMobil Research and Engineering Company Weichmachungsverfahren für fischer-tropschwachsen durch hydrobehandlung unter milden bedingungen
EP2075314A1 (de) 2007-12-11 2009-07-01 Shell Internationale Research Maatschappij B.V. Fettformulierungen
EP2078744A1 (de) 2008-01-10 2009-07-15 Shell Internationale Researchmaatschappij B.V. Kraftstoffzusammensetzungen
EP2078743A1 (de) 2008-01-10 2009-07-15 Shell Internationale Researchmaatschappij B.V. Kraftstoffzusammensetzung
EP2100946A1 (de) 2008-09-08 2009-09-16 Shell Internationale Researchmaatschappij B.V. Ölformulierungen
US7638661B2 (en) 2003-12-01 2009-12-29 Shell Oil Company Power increase and increase in acceleration performance of diesel fuel compositions
US7642294B2 (en) 2004-10-08 2010-01-05 Shell Oil Company Process to prepare lower olefins from a carbon containing feedstock
US7704375B2 (en) 2002-07-19 2010-04-27 Shell Oil Company Process for reducing corrosion in a condensing boiler burning liquid fuel
US7704378B2 (en) * 2003-01-27 2010-04-27 Institut Francais Du Petrole Method for the production of middle distillates by hydroisomerisation et hydrocracking of charges arising from the Fischer-Tropsch method
US7737311B2 (en) 2003-09-03 2010-06-15 Shell Oil Company Fuel compositions
WO2010076303A1 (en) 2008-12-29 2010-07-08 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2010076304A1 (en) 2008-12-29 2010-07-08 Shell Internationale Research Maatschappij B.V. Fuel compositions
US7757676B2 (en) 2005-03-01 2010-07-20 Shell Oil Company Reforming of GTL for marine applications
WO2010112691A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch mettant en oeuvre une resine
WO2010112690A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procédé de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
US7837853B2 (en) 2005-04-11 2010-11-23 Shell Oil Company Process to blend a mineral and a Fischer-Tropsch derived product onboard a marine vessel
US7867377B2 (en) 2005-12-22 2011-01-11 Shell Oil Company Fuel composition
WO2011023766A1 (en) 2009-08-28 2011-03-03 Shell Internationale Research Maatschappij B.V. Process oil composition
WO2011076948A1 (en) 2009-12-24 2011-06-30 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2011080250A1 (en) 2009-12-29 2011-07-07 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2011110551A1 (en) 2010-03-10 2011-09-15 Shell Internationale Research Maatschappij B.V. Method of reducing the toxicity of used lubricating compositions
EP2371931A1 (de) 2010-03-23 2011-10-05 Shell Internationale Research Maatschappij B.V. Kraftstoffzusammensetzungen
US8152868B2 (en) 2007-12-20 2012-04-10 Shell Oil Company Fuel compositions
US8152869B2 (en) 2007-12-20 2012-04-10 Shell Oil Company Fuel compositions
US8221614B2 (en) 2007-12-07 2012-07-17 Shell Oil Company Base oil formulations
EP0861311B2 (de) † 1995-10-17 2012-08-08 ExxonMobil Research and Engineering Company Verfahren zur herstellung synthetischer dieselbrennstoff
WO2012163935A2 (en) 2011-05-30 2012-12-06 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2013034617A1 (en) 2011-09-06 2013-03-14 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
EP2586852A1 (de) 2011-10-25 2013-05-01 Shell Internationale Research Maatschappij B.V. Verfahren zum Herstellen von Strahlenbrennstoffen und Produkte
EP2586851A1 (de) * 2011-10-27 2013-05-01 IFP Energies nouvelles Herstellungsverfahren von Mitteldestillaten, bei dem die aus dem Fischer-Tropsch-Verfahren hervorgegangene Charge und der Wasserstofffluss eine begrenzte Menge von Sauerstoff enthalten
US8444718B2 (en) 2006-03-29 2013-05-21 Shell Oil Company Process to prepare an aviation fuel
WO2013093080A1 (en) 2011-12-22 2013-06-27 Shell Internationale Research Maatschappij B.V. Improvements relating to high pressure compressor lubrication
US8475647B2 (en) 2005-08-22 2013-07-02 Shell Oil Company Diesel fuel and a method of operating a diesel engine
US8486876B2 (en) 2007-10-19 2013-07-16 Shell Oil Company Functional fluids for internal combustion engines
US8541635B2 (en) 2006-03-10 2013-09-24 Shell Oil Company Diesel fuel compositions
US8715371B2 (en) 2007-05-11 2014-05-06 Shell Oil Company Fuel composition
EP2738240A1 (de) 2012-11-30 2014-06-04 Schepers Handels- en domeinnamen B.V. Verwendung von Gas-to-Liquids-Gasöl in einer Lampenölzusammensetzung oder einem Feuerzeug
WO2014096169A1 (en) 2012-12-20 2014-06-26 Shell Internationale Research Maatschappij B.V. Fischer-tropsch derived fuel compositions
WO2014096234A1 (en) 2012-12-21 2014-06-26 Shell Internationale Research Maatschappij B.V. Liquid diesel fuel compositions containing organic sunscreen compounds
US8926716B2 (en) 2006-10-20 2015-01-06 Shell Oil Company Method of formulating a fuel composition
US20150021231A1 (en) * 2013-07-22 2015-01-22 Greyrock Energy, Inc. Blends of synthetic diesel fuel and petroleum diesel fuel with improved performance characteristics
WO2015071160A1 (en) 2013-11-18 2015-05-21 Total Marketing Services Process for the production of hydrocarbon fluids having a low aromatic and sulfur content
EP1927643A4 (de) * 2005-09-22 2015-05-27 Japan Oil Gas & Metals Jogmec Hydrierverfahren
WO2015091458A1 (en) 2013-12-16 2015-06-25 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
EP2889361A1 (de) 2013-12-31 2015-07-01 Shell Internationale Research Maatschappij B.V. Dieselkraftstoffformulierung und Verwendung davon
WO2015157207A1 (en) 2014-04-08 2015-10-15 Shell Oil Company Diesel fuel with improved ignition characteristics
EP2949732A1 (de) 2014-05-28 2015-12-02 Shell Internationale Research Maatschappij B.V. Verwendung einer oxanilid-verbindung in einer dieselkraftstoffzusammensetzung für den zweck der modifizierung der zündverzögerung und/oder der brenndauer
US9447356B2 (en) 2013-02-20 2016-09-20 Shell Oil Company Diesel fuel with improved ignition characteristics
EP3078728A1 (de) 2015-04-07 2016-10-12 Shell Internationale Research Maatschappij B.V. Viskositätsindexverbesserer für kraftstoffzusammensetzungen
EP3095842A1 (de) 2015-05-20 2016-11-23 Total Marketing Services Verfahren zur herstellung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten auf basis von syngas
WO2016188850A1 (en) 2015-05-22 2016-12-01 Shell Internationale Research Maatschappij B.V. Fuel composition
WO2016188858A1 (en) 2015-05-22 2016-12-01 Shell Internationale Research Maatschappij B.V. Fuel composition
WO2017050777A1 (en) 2015-09-22 2017-03-30 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2017081199A1 (en) 2015-11-11 2017-05-18 Shell Internationale Research Maatschappij B.V. Process for preparing a diesel fuel composition
US9663735B2 (en) 2013-10-24 2017-05-30 Shell Oil Company Liquid fuel compositions
WO2017093203A1 (en) 2015-11-30 2017-06-08 Shell Internationale Research Maatschappij B.V. Fuel composition
EP3184612A1 (de) 2015-12-21 2017-06-28 Shell Internationale Research Maatschappij B.V. Verfahren zur herstellung einer dieselkraftstoffzusammensetzung
WO2017134251A1 (en) 2016-02-05 2017-08-10 Shell Internationale Research Maatschappij B.V. Fuel composition
WO2017202735A1 (en) 2016-05-23 2017-11-30 Shell Internationale Research Maatschappij B.V. Use of a wax anti-settling additive in automotive fuel compositions
EP3315592A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten als bohrflüssigkeiten
EP3315590A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von kohlenwasserstoffflüssigkeiten in elektrischen fahrzeugen
EP3315586A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten als wärmeübertragungsmedien
WO2018077976A1 (en) 2016-10-27 2018-05-03 Shell Internationale Research Maatschappij B.V. Process for preparing an automotive gasoil
EP3342842A1 (de) 2017-01-03 2018-07-04 Total Marketing Services Entwachsungs- und entaromatisierungsverfahren von kohlenwasserstoff in einem schlammreaktor
WO2018206729A1 (en) 2017-05-11 2018-11-15 Shell Internationale Research Maatschappij B.V. Process for preparing an automotive gas oil fraction
WO2019007857A1 (en) 2017-07-03 2019-01-10 Shell Internationale Research Maatschappij B.V. USE OF A PARAFFINIC GASOLINE
US10294436B2 (en) 2014-11-12 2019-05-21 Shell Oil Company Fuel composition
US10407637B2 (en) 2015-08-17 2019-09-10 Shell Oil Company Fuel composition
WO2019201630A1 (en) 2018-04-20 2019-10-24 Shell Internationale Research Maatschappij B.V. Diesel fuel with improved ignition characteristics
WO2020007790A1 (en) 2018-07-02 2020-01-09 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2020070246A1 (en) 2018-10-05 2020-04-09 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2020109184A1 (en) 2018-11-26 2020-06-04 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2020120416A1 (en) 2018-12-11 2020-06-18 Shell Internationale Research Maatschappij B.V. Use and method to reduce deposits in compression ignition internal combustion engines
WO2021160694A1 (en) 2020-02-12 2021-08-19 Shell Internationale Research Maatschappij B.V. Use of a paraffinic gasoil
WO2022084281A1 (en) 2020-10-20 2022-04-28 Shell Internationale Research Maatschappij B.V. Use of a diesel fuel composition
WO2022122888A1 (en) 2020-12-11 2022-06-16 Shell Internationale Research Maatschappij B.V. Use of a detergent additive
WO2022122887A1 (en) 2020-12-11 2022-06-16 Shell Internationale Research Maatschappij B.V. Use of a paraffinic gasoil
WO2022228990A1 (en) 2021-04-26 2022-11-03 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2022228989A1 (en) 2021-04-26 2022-11-03 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2023066738A1 (en) 2021-10-20 2023-04-27 Shell Internationale Research Maatschappij B.V. Aviation fuel composition
WO2023174986A1 (en) 2022-03-17 2023-09-21 Shell Internationale Research Maatschappij B.V. Dual fuel engine system
US11851624B2 (en) 2021-10-20 2023-12-26 Shell Usa, Inc. Biofuel blends with improved oxidation stability and lubricity
WO2024040007A1 (en) 2022-08-15 2024-02-22 Energizer Auto, Inc. Surface treating formulation and method of making and using the same

Families Citing this family (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4811297A (en) * 1986-12-16 1989-03-07 Fujitsu Limited Boundary-free semiconductor memory device
CN100345896C (zh) 2002-08-12 2007-10-31 埃克森美孚化学专利公司 增塑聚烯烃组合物
US7271209B2 (en) 2002-08-12 2007-09-18 Exxonmobil Chemical Patents Inc. Fibers and nonwovens from plasticized polyolefin compositions
US7531594B2 (en) 2002-08-12 2009-05-12 Exxonmobil Chemical Patents Inc. Articles from plasticized polyolefin compositions
US7998579B2 (en) 2002-08-12 2011-08-16 Exxonmobil Chemical Patents Inc. Polypropylene based fibers and nonwovens
US8003725B2 (en) 2002-08-12 2011-08-23 Exxonmobil Chemical Patents Inc. Plasticized hetero-phase polyolefin blends
US8022108B2 (en) * 2003-07-02 2011-09-20 Chevron U.S.A. Inc. Acid treatment of a fischer-tropsch derived hydrocarbon stream
US8192813B2 (en) 2003-08-12 2012-06-05 Exxonmobil Chemical Patents, Inc. Crosslinked polyethylene articles and processes to produce same
US8158841B2 (en) 2004-03-25 2012-04-17 Japan Oil, Gas And Metals National Corporation Hydrotreating method
MY140997A (en) 2004-07-22 2010-02-12 Shell Int Research Process for the removal of cos from a synthesis gas stream comprising h2s and cos
US8389615B2 (en) 2004-12-17 2013-03-05 Exxonmobil Chemical Patents Inc. Elastomeric compositions comprising vinylaromatic block copolymer, polypropylene, plastomer, and low molecular weight polyolefin
US7851418B2 (en) 2005-06-03 2010-12-14 Exxonmobil Research And Engineering Company Ashless detergents and formulated lubricating oil containing same
EP1904576B1 (de) 2005-07-15 2012-04-25 ExxonMobil Chemical Patents Inc. Elastomere zusammensetzungen
US20070093398A1 (en) 2005-10-21 2007-04-26 Habeeb Jacob J Two-stroke lubricating oils
EA200801713A1 (ru) 2006-01-18 2008-12-30 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ удаления карбонилсульфида и сероводорода из потока синтез-газа
JP4834438B2 (ja) * 2006-03-30 2011-12-14 Ｊｘ日鉱日石エネルギー株式会社 燃料基材の水素化精製方法
US8299005B2 (en) 2006-05-09 2012-10-30 Exxonmobil Research And Engineering Company Lubricating oil composition
US7863229B2 (en) 2006-06-23 2011-01-04 Exxonmobil Research And Engineering Company Lubricating compositions
WO2009041508A1 (ja) * 2007-09-28 2009-04-02 Japan Oil, Gas And Metals National Corporation 合成ナフサの製造方法
CN101932679A (zh) * 2008-01-02 2010-12-29 国际壳牌研究有限公司 液体燃料组合物
JP5483045B2 (ja) * 2008-06-20 2014-05-07 独立行政法人産業技術総合研究所 一酸化炭素と水素からの炭化水素の製造方法
US20120004329A1 (en) * 2009-03-27 2012-01-05 Marie Iwama Liquid fuel producing method and liquid fuel producing system
GB201000971D0 (en) * 2010-01-21 2010-03-10 Johnson Matthey Plc Process for the convertion of synthesis gas
JP5443206B2 (ja) * 2010-02-24 2014-03-19 独立行政法人石油天然ガス・金属鉱物資源機構 水素化分解方法
US8968427B2 (en) 2010-12-24 2015-03-03 Shell Oil Company Blending fuels
AU2011232735C1 (en) * 2011-04-02 2015-10-08 Wanhua Industrial Group Co., Ltd. A high-selectivity catalyst for the production of high-quality gasoline fractions from syngas and its preparation method
FR2981360B1 (fr) 2011-10-14 2015-08-07 IFP Energies Nouvelles Procede de production de distillats moyens a partir d'un melange d'une charge issue de sources renouvelables et d'un effluent paraffinique
WO2013147190A1 (ja) * 2012-03-30 2013-10-03 Ｊｘ日鉱日石エネルギー株式会社 炭化水素油の脱蝋方法及び潤滑油用基油の製造方法
RU2656601C1 (ru) * 2017-08-08 2018-06-06 Публичное акционерное общество "Нефтяная компания "Роснефть" (ПАО "НК "Роснефть") Способ получения синтетической нефти

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4080397A (en) * 1976-07-09 1978-03-21 Mobile Oil Corporation Method for upgrading synthetic oils boiling above gasoline boiling material
US4423265A (en) * 1982-12-01 1983-12-27 Mobil Oil Corporation Process for snygas conversions to liquid hydrocarbon products
EP0370757A1 (de) * 1988-11-23 1990-05-30 Exxon Research And Engineering Company Titaniumoxyd enthaltende Katalysatoren, ihre Herstellung und Verwendung zur Fischer-Tropsch-Synthese

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL8003313A (nl) † 1980-06-06 1982-01-04 Shell Int Research Werkwijze voor de bereiding van middeldestillaten.
US4522939A (en) † 1983-05-31 1985-06-11 Shell Oil Company Preparation of catalyst for producing middle distillates from syngas
IN161735B (de) † 1983-09-12 1988-01-30 Shell Int Research
US4919786A (en) † 1987-12-18 1990-04-24 Exxon Research And Engineering Company Process for the hydroisomerization of was to produce middle distillate products (OP-3403)
US4943672A (en) † 1987-12-18 1990-07-24 Exxon Research And Engineering Company Process for the hydroisomerization of Fischer-Tropsch wax to produce lubricating oil (OP-3403)
US5028634A (en) * 1989-08-23 1991-07-02 Exxon Research & Engineering Company Two stage process for hydrocarbon synthesis
FR2676750B1 (fr) † 1991-05-21 1993-08-13 Inst Francais Du Petrole Procede d'hydrocraquage de paraffines issue du procede fischer-tropsch a l'aide de catalyseurs a base de zeolithe h-y.
US5378348A (en) † 1993-07-22 1995-01-03 Exxon Research And Engineering Company Distillate fuel production from Fischer-Tropsch wax

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4080397A (en) * 1976-07-09 1978-03-21 Mobile Oil Corporation Method for upgrading synthetic oils boiling above gasoline boiling material
US4423265A (en) * 1982-12-01 1983-12-27 Mobil Oil Corporation Process for snygas conversions to liquid hydrocarbon products
EP0370757A1 (de) * 1988-11-23 1990-05-30 Exxon Research And Engineering Company Titaniumoxyd enthaltende Katalysatoren, ihre Herstellung und Verwendung zur Fischer-Tropsch-Synthese

Cited By (165)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0668342A1 (de) * 1994-02-08 1995-08-23 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung von Basisschmieröl
SG94676A1 (en) * 1994-02-08 2003-03-18 Shell Int Research Lubricating base oil preparation process
EP0861311B2 (de) † 1995-10-17 2012-08-08 ExxonMobil Research and Engineering Company Verfahren zur herstellung synthetischer dieselbrennstoff
WO1999041217A1 (en) * 1998-02-13 1999-08-19 Exxon Research And Engineering Company Gas conversion using synthesis gas produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
US6043288A (en) * 1998-02-13 2000-03-28 Exxon Research And Engineering Co. Gas conversion using synthesis gas produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
USRE38170E1 (en) * 1998-02-13 2003-07-01 Exxonmobil Research And Engineering Company Gas conversion using synthesis gas produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
US6121333A (en) * 1998-06-25 2000-09-19 Agip Petroli S.P.A. Process for the preparation of hydrocarbons from synthesis gas
EP1088879A1 (de) * 1999-09-30 2001-04-04 Institut Francais Du Petrole Verfahren zur Erzeugung von Benzin mit verbesserter Oktanzahl
FR2799202A1 (fr) * 1999-09-30 2001-04-06 Inst Francais Du Petrole Procede de production d'essences a indice d'octane ameliore
US6436278B1 (en) 1999-09-30 2002-08-20 Institut Francais Du Petrole Process for producing gasoline with an improved octane number
US6544407B1 (en) * 1999-11-19 2003-04-08 Agip Petroli S.P.A. Process for the preparation of middle distillates starting from linear paraffins
US6497812B1 (en) 1999-12-22 2002-12-24 Chevron U.S.A. Inc. Conversion of C1-C3 alkanes and fischer-tropsch products to normal alpha olefins and other liquid hydrocarbons
EP1268712B2 (de) † 2000-04-04 2009-06-10 ExxonMobil Research and Engineering Company Weichmachungsverfahren für fischer-tropschwachsen durch hydrobehandlung unter milden bedingungen
EP1272592B1 (de) * 2000-04-04 2004-09-29 ExxonMobil Research and Engineering Company Verfahren zum einstellen der härte von fischer-tropschwachs durch mischung
GB2369370B (en) * 2000-10-23 2003-04-16 Chevron Usa Inc Method for retarding fouling of feed heaters in refinery processing
GB2369370A (en) * 2000-10-23 2002-05-29 Chevron Usa Inc Addition of hydrogen to hydrocarbon streams to prevent fouling
US6908543B1 (en) 2000-10-23 2005-06-21 Chevron U.S.A. Inc. Method for retarding fouling of feed heaters in refinery processing
US6900366B2 (en) 2001-01-11 2005-05-31 Chevron U.S.A. Inc. Process for upgrading of Fischer-Tropsch products
US6635171B2 (en) 2001-01-11 2003-10-21 Chevron U.S.A. Inc. Process for upgrading of Fischer-Tropsch products
US6858127B2 (en) 2001-03-05 2005-02-22 Shell Oil Company Process for the preparation of middle distillates
US6515032B2 (en) 2001-05-11 2003-02-04 Chevron U.S.A. Inc. Co-hydroprocessing of fischer-tropsch products and natural gas well condensate
US7404890B2 (en) 2001-07-06 2008-07-29 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the Fischer-Tropsch process
US7326331B2 (en) * 2001-07-06 2008-02-05 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking feeds from the fischer-tropsch process
US7220349B2 (en) 2001-07-06 2007-05-22 Institut Francais Du Petrole Process for the production of middle distillates by two-step hydroisomerisation and hydrocracking of feeds from the Fischer-Tropsch process
US7156978B2 (en) * 2001-07-06 2007-01-02 Institut Francais Du Petrole Process for the production of middle distillates by hydroisomerisation and hydrocracking of two fractions from feeds originating from the fischer-tropsch process
US6709569B2 (en) 2001-12-21 2004-03-23 Chevron U.S.A. Inc. Methods for pre-conditioning fischer-tropsch light products preceding upgrading
GB2386904B (en) * 2002-01-31 2005-02-23 Chevron Usa Inc Upgrading fischer-tropsch and petroleum-derived naphthas and distillates
US6863802B2 (en) 2002-01-31 2005-03-08 Chevron U.S.A. Upgrading fischer-Tropsch and petroleum-derived naphthas and distillates
US7033552B2 (en) 2002-01-31 2006-04-25 Chevron U.S.A. Inc. Upgrading Fischer-Tropsch and petroleum-derived naphthas and distillates
US7704375B2 (en) 2002-07-19 2010-04-27 Shell Oil Company Process for reducing corrosion in a condensing boiler burning liquid fuel
US7189269B2 (en) 2002-10-18 2007-03-13 Shell Oil Company Fuel composition comprising a base fuel, a fischer tropsch derived gas oil, and an oxygenate
US7229481B2 (en) 2002-11-13 2007-06-12 Shell Oil Company Diesel fuel compositions
US7704378B2 (en) * 2003-01-27 2010-04-27 Institut Francais Du Petrole Method for the production of middle distillates by hydroisomerisation et hydrocracking of charges arising from the Fischer-Tropsch method
WO2004074406A1 (en) * 2003-02-18 2004-09-02 Chevron U.S.A. Inc. Process for producing premium fischer-tropsch diesel and lube base oils
US6939999B2 (en) 2003-02-24 2005-09-06 Syntroleum Corporation Integrated Fischer-Tropsch process with improved alcohol processing capability
US7151163B2 (en) 2003-04-28 2006-12-19 Sequoia Pharmaceuticals, Inc. Antiviral agents for the treatment, control and prevention of infections by coronaviruses
US6982355B2 (en) 2003-08-25 2006-01-03 Syntroleum Corporation Integrated Fischer-Tropsch process for production of linear and branched alcohols and olefins
US7737311B2 (en) 2003-09-03 2010-06-15 Shell Oil Company Fuel compositions
WO2005026297A1 (en) 2003-09-17 2005-03-24 Shell Internationale Research Maatschappij B.V. Petroleum- and fischer-tropsch- derived kerosene blend
US7666294B2 (en) 2003-09-17 2010-02-23 Shell Oil Company Depressed freeze point kerosene fuel compositions and methods of making and using same
US7638661B2 (en) 2003-12-01 2009-12-29 Shell Oil Company Power increase and increase in acceleration performance of diesel fuel compositions
US7354507B2 (en) 2004-03-17 2008-04-08 Conocophillips Company Hydroprocessing methods and apparatus for use in the preparation of liquid hydrocarbons
WO2006010068A1 (en) * 2004-07-08 2006-01-26 Conocophillips Company Synthetic hydrocarbon products
US7345211B2 (en) 2004-07-08 2008-03-18 Conocophillips Company Synthetic hydrocarbon products
US7642294B2 (en) 2004-10-08 2010-01-05 Shell Oil Company Process to prepare lower olefins from a carbon containing feedstock
US7757676B2 (en) 2005-03-01 2010-07-20 Shell Oil Company Reforming of GTL for marine applications
US7837853B2 (en) 2005-04-11 2010-11-23 Shell Oil Company Process to blend a mineral and a Fischer-Tropsch derived product onboard a marine vessel
FR2888584A1 (fr) * 2005-07-18 2007-01-19 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage de charges issues du procede fischer-tropsch utilisant un lit de garde multifonctionnel
US7658836B2 (en) 2005-07-18 2010-02-09 Institut Francais Du Petrole Process for producing middle distillates by hydroisomerizing and hydrocracking feeds from the Fischer-Tropsch process using a multifunctional guard bed
WO2007010126A3 (fr) * 2005-07-18 2007-03-15 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage de charges issues du procede fischer-tropsch utilisant un lit de garde multifonctionnel
WO2007009987A1 (en) * 2005-07-20 2007-01-25 Shell Internationale Research Maatschappij B.V. Hydrocarbon synthesis process
US8475647B2 (en) 2005-08-22 2013-07-02 Shell Oil Company Diesel fuel and a method of operating a diesel engine
EP1927643A4 (de) * 2005-09-22 2015-05-27 Japan Oil Gas & Metals Jogmec Hydrierverfahren
US7867377B2 (en) 2005-12-22 2011-01-11 Shell Oil Company Fuel composition
US8541635B2 (en) 2006-03-10 2013-09-24 Shell Oil Company Diesel fuel compositions
US8444718B2 (en) 2006-03-29 2013-05-21 Shell Oil Company Process to prepare an aviation fuel
CN101410490A (zh) * 2006-03-31 2009-04-15 新日本石油株式会社 蜡的加氢裂化方法和燃料基材的制造方法
CN101410490B (zh) * 2006-03-31 2013-05-29 新日本石油株式会社 蜡的加氢裂化方法和燃料基材的制造方法
AU2007232039B2 (en) * 2006-03-31 2011-09-29 Nippon Oil Corporation Method for hydrocracking wax and method for producing fuel base material
US8926716B2 (en) 2006-10-20 2015-01-06 Shell Oil Company Method of formulating a fuel composition
US8715371B2 (en) 2007-05-11 2014-05-06 Shell Oil Company Fuel composition
FR2917419A1 (fr) * 2007-06-12 2008-12-19 Inst Francais Du Petrole Procede de production de distilltats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
WO2009004179A3 (fr) * 2007-06-12 2009-02-19 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
US8709234B2 (en) 2007-06-12 2014-04-29 IFP Energies Nouvelles Process for producing middle distillates by hydroismerizing and hydrocracking a heavy fraction from a fischer-tropsch effluent
US8486876B2 (en) 2007-10-19 2013-07-16 Shell Oil Company Functional fluids for internal combustion engines
US8221614B2 (en) 2007-12-07 2012-07-17 Shell Oil Company Base oil formulations
EP2075314A1 (de) 2007-12-11 2009-07-01 Shell Internationale Research Maatschappij B.V. Fettformulierungen
US9556396B2 (en) 2007-12-11 2017-01-31 Shell Oil Company Grease formulations
US8152868B2 (en) 2007-12-20 2012-04-10 Shell Oil Company Fuel compositions
US8152869B2 (en) 2007-12-20 2012-04-10 Shell Oil Company Fuel compositions
US8273137B2 (en) 2008-01-10 2012-09-25 Shell Oil Company Fuel composition
EP2078744A1 (de) 2008-01-10 2009-07-15 Shell Internationale Researchmaatschappij B.V. Kraftstoffzusammensetzungen
EP2078743A1 (de) 2008-01-10 2009-07-15 Shell Internationale Researchmaatschappij B.V. Kraftstoffzusammensetzung
EP2100946A1 (de) 2008-09-08 2009-09-16 Shell Internationale Researchmaatschappij B.V. Ölformulierungen
WO2010076303A1 (en) 2008-12-29 2010-07-08 Shell Internationale Research Maatschappij B.V. Fuel compositions
US9017429B2 (en) 2008-12-29 2015-04-28 Shell Oil Company Fuel compositions
WO2010076304A1 (en) 2008-12-29 2010-07-08 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2010112691A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch mettant en oeuvre une resine
FR2944027A1 (fr) * 2009-04-03 2010-10-08 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
FR2944028A1 (fr) * 2009-04-03 2010-10-08 Inst Francais Du Petrole Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch mettant en oeuvre une resine
WO2010112690A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procédé de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
WO2011023766A1 (en) 2009-08-28 2011-03-03 Shell Internationale Research Maatschappij B.V. Process oil composition
WO2011076948A1 (en) 2009-12-24 2011-06-30 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2011080250A1 (en) 2009-12-29 2011-07-07 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2011110551A1 (en) 2010-03-10 2011-09-15 Shell Internationale Research Maatschappij B.V. Method of reducing the toxicity of used lubricating compositions
US8876923B2 (en) 2010-03-23 2014-11-04 Shell Oil Company Fuel compositions
EP2371931A1 (de) 2010-03-23 2011-10-05 Shell Internationale Research Maatschappij B.V. Kraftstoffzusammensetzungen
WO2012163935A2 (en) 2011-05-30 2012-12-06 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
WO2013034617A1 (en) 2011-09-06 2013-03-14 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
EP2586852A1 (de) 2011-10-25 2013-05-01 Shell Internationale Research Maatschappij B.V. Verfahren zum Herstellen von Strahlenbrennstoffen und Produkte
FR2981944A1 (fr) * 2011-10-27 2013-05-03 IFP Energies Nouvelles Procede de production de distillats moyens dans lequel la charge issue du procede fischer-tropsch et le flux d'hydrogene contiennent une teneur limitee en oxygene
EP2586851A1 (de) * 2011-10-27 2013-05-01 IFP Energies nouvelles Herstellungsverfahren von Mitteldestillaten, bei dem die aus dem Fischer-Tropsch-Verfahren hervorgegangene Charge und der Wasserstofffluss eine begrenzte Menge von Sauerstoff enthalten
US9546329B2 (en) 2011-10-27 2017-01-17 IFP Energies Nouvelles Process for the production of middle distillates in which the feedstock originating from the fischer-tropsch process and the hydrogen stream contain a limited oxygen content
WO2013093080A1 (en) 2011-12-22 2013-06-27 Shell Internationale Research Maatschappij B.V. Improvements relating to high pressure compressor lubrication
EP2738240A1 (de) 2012-11-30 2014-06-04 Schepers Handels- en domeinnamen B.V. Verwendung von Gas-to-Liquids-Gasöl in einer Lampenölzusammensetzung oder einem Feuerzeug
WO2014096169A1 (en) 2012-12-20 2014-06-26 Shell Internationale Research Maatschappij B.V. Fischer-tropsch derived fuel compositions
US10041013B2 (en) 2012-12-20 2018-08-07 Shell Oil Company Fischer-Tropsch derived fuel compositions
US9222047B2 (en) 2012-12-21 2015-12-29 Shell Oil Company Liquid fuel compositions
WO2014096234A1 (en) 2012-12-21 2014-06-26 Shell Internationale Research Maatschappij B.V. Liquid diesel fuel compositions containing organic sunscreen compounds
US9447356B2 (en) 2013-02-20 2016-09-20 Shell Oil Company Diesel fuel with improved ignition characteristics
US20150021231A1 (en) * 2013-07-22 2015-01-22 Greyrock Energy, Inc. Blends of synthetic diesel fuel and petroleum diesel fuel with improved performance characteristics
US9663735B2 (en) 2013-10-24 2017-05-30 Shell Oil Company Liquid fuel compositions
WO2015071160A1 (en) 2013-11-18 2015-05-21 Total Marketing Services Process for the production of hydrocarbon fluids having a low aromatic and sulfur content
WO2015091458A1 (en) 2013-12-16 2015-06-25 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
US9587195B2 (en) 2013-12-16 2017-03-07 Shell Oil Company Liquid composition
EP2889361A1 (de) 2013-12-31 2015-07-01 Shell Internationale Research Maatschappij B.V. Dieselkraftstoffformulierung und Verwendung davon
US9862905B2 (en) 2014-04-08 2018-01-09 Shell Oil Company Diesel fuel with improved ignition characteristics
WO2015157207A1 (en) 2014-04-08 2015-10-15 Shell Oil Company Diesel fuel with improved ignition characteristics
EP2949732A1 (de) 2014-05-28 2015-12-02 Shell Internationale Research Maatschappij B.V. Verwendung einer oxanilid-verbindung in einer dieselkraftstoffzusammensetzung für den zweck der modifizierung der zündverzögerung und/oder der brenndauer
US10294436B2 (en) 2014-11-12 2019-05-21 Shell Oil Company Fuel composition
EP3078728A1 (de) 2015-04-07 2016-10-12 Shell Internationale Research Maatschappij B.V. Viskositätsindexverbesserer für kraftstoffzusammensetzungen
EP3095842A1 (de) 2015-05-20 2016-11-23 Total Marketing Services Verfahren zur herstellung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten auf basis von syngas
WO2016188850A1 (en) 2015-05-22 2016-12-01 Shell Internationale Research Maatschappij B.V. Fuel composition
US11104857B2 (en) 2015-05-22 2021-08-31 Shell Oil Company Fuel composition
US11001775B2 (en) 2015-05-22 2021-05-11 Shell Oil Company Fuel composition
WO2016188858A1 (en) 2015-05-22 2016-12-01 Shell Internationale Research Maatschappij B.V. Fuel composition
US10407637B2 (en) 2015-08-17 2019-09-10 Shell Oil Company Fuel composition
WO2017050777A1 (en) 2015-09-22 2017-03-30 Shell Internationale Research Maatschappij B.V. Fuel compositions
US10808195B2 (en) 2015-09-22 2020-10-20 Shell Oil Company Fuel compositions
WO2017081199A1 (en) 2015-11-11 2017-05-18 Shell Internationale Research Maatschappij B.V. Process for preparing a diesel fuel composition
US11084997B2 (en) 2015-11-11 2021-08-10 Shell Oil Company Process for preparing a diesel fuel composition
EP3397734B1 (de) 2015-11-30 2020-07-29 Shell International Research Maatschappij B.V. Kraftstoffzusammensetzung
US11959033B2 (en) 2015-11-30 2024-04-16 Shell Usa, Inc. Fuel composition
WO2017093203A1 (en) 2015-11-30 2017-06-08 Shell Internationale Research Maatschappij B.V. Fuel composition
EP3184612A1 (de) 2015-12-21 2017-06-28 Shell Internationale Research Maatschappij B.V. Verfahren zur herstellung einer dieselkraftstoffzusammensetzung
US11254885B2 (en) 2016-02-05 2022-02-22 Shell Oil Company Fuel composition
WO2017134251A1 (en) 2016-02-05 2017-08-10 Shell Internationale Research Maatschappij B.V. Fuel composition
WO2017202735A1 (en) 2016-05-23 2017-11-30 Shell Internationale Research Maatschappij B.V. Use of a wax anti-settling additive in automotive fuel compositions
US11359155B2 (en) 2016-05-23 2022-06-14 Shell Usa, Inc. Use of a wax anti-settling additive in automotive fuel compositions
WO2018078023A1 (en) 2016-10-27 2018-05-03 Total Marketing Services Use of biodegradable hydrocarbon fluids as drilling fluids
WO2018078024A1 (en) 2016-10-27 2018-05-03 Total Marketing Services Use of biodegradable hydrocarbon fluids in electric vehicles
EP3315586A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten als wärmeübertragungsmedien
WO2018078021A1 (en) 2016-10-27 2018-05-03 Total Marketing Services Use of biodegradable hydrocarbon fluids as heat-transfer media
US11981854B2 (en) 2016-10-27 2024-05-14 Total Marketing Services Use of biodegradable hydrocarbon fluids as drilling fluids
WO2018077976A1 (en) 2016-10-27 2018-05-03 Shell Internationale Research Maatschappij B.V. Process for preparing an automotive gasoil
US11680196B2 (en) 2016-10-27 2023-06-20 Total Marketing Services Use of biodegradable hydrocarbon fluids as heat-transfer media
EP3315592A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von biologisch abbaubaren kohlenwasserstoffflüssigkeiten als bohrflüssigkeiten
EP3315590A1 (de) 2016-10-27 2018-05-02 Total Marketing Services Verwendung von kohlenwasserstoffflüssigkeiten in elektrischen fahrzeugen
US11066589B2 (en) 2016-10-27 2021-07-20 Total Marketing Services Use of biodegradable hydrocarbon fluids as drilling fluids
US11021669B2 (en) 2016-10-27 2021-06-01 Total Marketing Services Use of biodegradable hydrocarbon fluids in electric vehicles
EP3342842A1 (de) 2017-01-03 2018-07-04 Total Marketing Services Entwachsungs- und entaromatisierungsverfahren von kohlenwasserstoff in einem schlammreaktor
WO2018127458A1 (en) 2017-01-03 2018-07-12 Total Marketing Services Dewaxing and dearomatization process of hydrocarbon in a slurry reactor
US11248179B2 (en) 2017-01-03 2022-02-15 Total Marketing Services Dewaxing and dearomatization process of hydrocarbon in a slurry reactor
WO2018206729A1 (en) 2017-05-11 2018-11-15 Shell Internationale Research Maatschappij B.V. Process for preparing an automotive gas oil fraction
US11634652B2 (en) 2017-07-03 2023-04-25 Shell Usa, Inc. Use of a paraffinic gasoil
WO2019007857A1 (en) 2017-07-03 2019-01-10 Shell Internationale Research Maatschappij B.V. USE OF A PARAFFINIC GASOLINE
WO2019201630A1 (en) 2018-04-20 2019-10-24 Shell Internationale Research Maatschappij B.V. Diesel fuel with improved ignition characteristics
US11512261B2 (en) 2018-04-20 2022-11-29 Shell Usa, Inc. Diesel fuel with improved ignition characteristics
WO2020007790A1 (en) 2018-07-02 2020-01-09 Shell Internationale Research Maatschappij B.V. Liquid fuel compositions
US11499107B2 (en) 2018-07-02 2022-11-15 Shell Usa, Inc. Liquid fuel compositions
WO2020070246A1 (en) 2018-10-05 2020-04-09 Shell Internationale Research Maatschappij B.V. Fuel compositions
US11499106B2 (en) 2018-11-26 2022-11-15 Shell Usa, Inc. Fuel compositions
WO2020109184A1 (en) 2018-11-26 2020-06-04 Shell Internationale Research Maatschappij B.V. Fuel compositions
US11867117B2 (en) 2018-12-11 2024-01-09 Shell Usa, Inc. Use and method to reduce deposits in compression ignition internal combustion engines
WO2020120416A1 (en) 2018-12-11 2020-06-18 Shell Internationale Research Maatschappij B.V. Use and method to reduce deposits in compression ignition internal combustion engines
WO2021160694A1 (en) 2020-02-12 2021-08-19 Shell Internationale Research Maatschappij B.V. Use of a paraffinic gasoil
WO2022084281A1 (en) 2020-10-20 2022-04-28 Shell Internationale Research Maatschappij B.V. Use of a diesel fuel composition
WO2022122888A1 (en) 2020-12-11 2022-06-16 Shell Internationale Research Maatschappij B.V. Use of a detergent additive
WO2022122887A1 (en) 2020-12-11 2022-06-16 Shell Internationale Research Maatschappij B.V. Use of a paraffinic gasoil
WO2022228990A1 (en) 2021-04-26 2022-11-03 Shell Internationale Research Maatschappij B.V. Fuel compositions
WO2022228989A1 (en) 2021-04-26 2022-11-03 Shell Internationale Research Maatschappij B.V. Fuel compositions
US11851624B2 (en) 2021-10-20 2023-12-26 Shell Usa, Inc. Biofuel blends with improved oxidation stability and lubricity
WO2023066738A1 (en) 2021-10-20 2023-04-27 Shell Internationale Research Maatschappij B.V. Aviation fuel composition
WO2023174986A1 (en) 2022-03-17 2023-09-21 Shell Internationale Research Maatschappij B.V. Dual fuel engine system
WO2024040007A1 (en) 2022-08-15 2024-02-22 Energizer Auto, Inc. Surface treating formulation and method of making and using the same

Also Published As

Publication number Publication date
AU4467693A (en) 1994-02-24
JP3522797B2 (ja) 2004-04-26
MY108862A (en) 1996-11-30
RU2101324C1 (ru) 1998-01-10
JPH06158058A (ja) 1994-06-07
NZ248415A (en) 1995-03-28
DE69314879T2 (de) 1998-03-12
NO305288B1 (no) 1999-05-03
ES2110051T3 (es) 1998-02-01
NO932905L (no) 1994-02-21
CA2104158A1 (en) 1994-02-19
DZ1708A1 (fr) 2002-02-17
AU666960B2 (en) 1996-02-29
DK0583836T3 (da) 1998-03-02
DE69314879D1 (de) 1997-12-04
DE69314879T3 (de) 2002-07-18
ES2110051T5 (es) 2002-10-01
NO932905D0 (no) 1993-08-16
EP0583836B1 (de) 1997-10-29
DK0583836T4 (da) 2002-03-11
ZA935964B (en) 1994-03-15
EP0583836B2 (de) 2002-02-13
CA2104158C (en) 2005-11-15

Similar Documents

Publication Publication Date Title
EP0583836B2 (de) Verfahren zur Herstellung von Kohlenwasserstoffbrennstoffen
US5371308A (en) Process for the preparation of lower olefins
EP0668342B1 (de) Verfahren zur Herstellung von Basisschmieröl
US5888376A (en) Conversion of fischer-tropsch light oil to jet fuel by countercurrent processing
JP4181876B2 (ja) 分割フィード水素化分解／水素化処理を用いるフィッシャー−トロプシュワックスの改質法
EP0211593B1 (de) Verfahren zur Entfernung von polynuklearen aromatischen Kohlenwasserstoffverbindungen aus Mischungen von flüssigen Kohlenwasserstoffverbindungen
US20020082166A1 (en) Process for the preparation of high activity carbon monoxide hydrogenation catalysts; the catalyst compositions, use of the catalysts for conducting such reactions, and the products of such reactions
US5498821A (en) Carbon dioxide addition in hydrocracking/hydroisomerization processes to control methane production
US20010006984A1 (en) Process for the reactivation of sulfur deactivated cobalt titania catalysts; the catalyst compositions, use of the reactivated catalysts for conducting carbon monoxide hydrogenation, reactions and the products of such reactions
WO2007082589A1 (en) Hydrogenation catalyst and use thereof for hdrogenating fischer-tropsch endproducts
EP1268712B1 (de) Weichmachungsverfahren für fischer-tropschwachsen durch hydrobehandlung unter milden bedingungen
US20020028745A1 (en) Process for the preparation of high activity carbon monoxide hydrogenation catalysts; the catalyst compositions, use of the catalysts for conducting such reactions, and the products of such reactions
AU2002337372B2 (en) Olefins production process
ZA200600307B (en) Process for the oligomerization of olefins in Fischer-Tropsch derived feeds
EP0707057B1 (de) Addition von Kohlendioxid in Hydrokrack/Hydroisomerizierungsverfahren zur Kontrolierung der Methanherstellung
CA2141925C (en) Lubricating base oil preparation process
US6515033B2 (en) Methods for optimizing fischer-tropsch synthesis hydrocarbons in the distillate fuel range
AU702829B2 (en) Hydroisomerization of waxy hydrocarbon feeds over a slurried catalyst
US3773656A (en) Process for hydrocarbon cracking using a tungsten-rhenium catalyst

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE DK ES FR GB IT NL SE

17P Request for examination filed

Effective date: 19940615

17Q First examination report despatched

Effective date: 19960205

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE DK ES FR GB IT NL SE

ITF It: translation for a ep patent filed
REF Corresponds to:

Ref document number: 69314879

Country of ref document: DE

Date of ref document: 19971204

ET Fr: translation filed
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2110051

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

26 Opposition filed

Opponent name: CHEVRON U.S.A. INC.

Effective date: 19980729

NLR1 Nl: opposition has been filed with the epo

Opponent name: CHEVRON U.S.A. INC.

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

PLAB Opposition data, opponent's data or that of the opponent's representative modified

Free format text: ORIGINAL CODE: 0009299OPPO

R26 Opposition filed (corrected)

Opponent name: CHEVRON U.S.A. INC.

Effective date: 19980729

NLR1 Nl: opposition has been filed with the epo

Opponent name: CHEVRON U.S.A. INC.

PLAW Interlocutory decision in opposition

Free format text: ORIGINAL CODE: EPIDOS IDOP

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

APAE Appeal reference modified

Free format text: ORIGINAL CODE: EPIDOS REFNO

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

PLAW Interlocutory decision in opposition

Free format text: ORIGINAL CODE: EPIDOS IDOP

PUAH Patent maintained in amended form

Free format text: ORIGINAL CODE: 0009272

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: PATENT MAINTAINED AS AMENDED

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

27A Patent maintained in amended form

Effective date: 20020213

AK Designated contracting states

Kind code of ref document: B2

Designated state(s): BE DE DK ES FR GB IT NL SE

REG Reference to a national code

Ref country code: DK

Ref legal event code: T4

NLR2 Nl: decision of opposition
NLR3 Nl: receipt of modified translations in the netherlands language after an opposition procedure
ET3 Fr: translation filed ** decision concerning opposition
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20020809

Year of fee payment: 10

REG Reference to a national code

Ref country code: ES

Ref legal event code: DC2A

Kind code of ref document: T5

Effective date: 20020513

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20030610

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20030626

Year of fee payment: 11

Ref country code: DK

Payment date: 20030626

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20030723

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20030811

Year of fee payment: 11

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040817

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040817

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040831

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040831

BERE Be: lapsed

Owner name: *SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.

Effective date: 20040831

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20050301

EUG Se: european patent has lapsed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20050429

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20050301

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20050816

APAH Appeal reference modified

Free format text: ORIGINAL CODE: EPIDOSCREFNO

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20040817

BERE Be: lapsed

Owner name: *SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.

Effective date: 20040831

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20080901

Year of fee payment: 16

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20080711

Year of fee payment: 16

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20090816

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20100302

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090816