EP1926802A1 - Procede de melange d' un produit hydrocarbone derive d' un mineral et d' un produit hydrocarbone derive de fisher-tropsch - Google Patents

Procede de melange d' un produit hydrocarbone derive d' un mineral et d' un produit hydrocarbone derive de fisher-tropsch

Info

Publication number
EP1926802A1
EP1926802A1 EP20060793664 EP06793664A EP1926802A1 EP 1926802 A1 EP1926802 A1 EP 1926802A1 EP 20060793664 EP20060793664 EP 20060793664 EP 06793664 A EP06793664 A EP 06793664A EP 1926802 A1 EP1926802 A1 EP 1926802A1
Authority
EP
European Patent Office
Prior art keywords
fischer
mineral
derived
blend
hydrocarbon product
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.)
Ceased
Application number
EP20060793664
Other languages
German (de)
English (en)
Inventor
Claire Ansell
Richard Hugh Clark
Richard John Heins
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
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to EP20060793664 priority Critical patent/EP1926802A1/fr
Publication of EP1926802A1 publication Critical patent/EP1926802A1/fr
Ceased 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
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Definitions

  • the present invention relates to a process to blend a mineral derived hydrocarbon product and a Fischer-Tropsch derived hydrocarbon product.
  • WO-A-03/087273 This publication describes that a mineral derived gas oil may be blended in a refinery environment to achieve a blended product having a certain cetane number .
  • WO-A-03/087273 provides a process to achieve a blend having a certain quality property it can still be improved in terms of the blending operation itself. The present process provides such a solution.
  • a fully blended product can be obtained by the process according to the invention.
  • the following process makes available a blended product suited for direct use at for example a refinery environment .
  • a process to blend a mineral derived hydrocarbon product and a Fischer-Tropsch derived hydrocarbon product by providing in an Above Ground Storage Tank a quantity of mineral derived hydrocarbon product and Fischer-Tropsch derived hydrocarbon product such that initially the mineral derived hydrocarbon product is located substantially above the Fischer- Tropsch derived hydrocarbon product.
  • the Fischer-Tropsch derived hydrocarbon product is suitably obtained by converting a mixture of carbon monoxide and hydrogen in the presence of a suitable Fischer-Tropsch catalyst under Fischer-Tropsch operating conditions.
  • the catalysts used for the catalytic conversion of the mixture comprising hydrogen and carbon monoxide into the Fischer-Tropsch derived paraffinic hydrocarbon product are known in the art.
  • Catalysts for use in this process frequently comprise, as the catalytically active component, a metal from Group VIII of the Periodic Table of Elements .
  • Particular catalytically active metals include ruthenium, iron, cobalt and nickel. Cobalt is a preferred catalytically active metal.
  • Fischer-Tropsch synthesis processes are the so-called commercial Sasol process, the Shell Middle Distillate Synthesis Process and the AGC-21 ExxonMobil process. These and other processes are for example described in more detail in EP-A-0776959, EP-A-0668342, US-A-4943672, US-A-5059299, WO-A-99/34917 and WO-A-99/20720.
  • the Fischer-Tropsch process may be carried out in a slurry reactor, a fixed bed reactor, especially a multitubular fixed bed reactor, or in a three phase fluidised bed reactor.
  • Syngas i.e. the mixture of carbon monoxide and hydrogen used in the Fischer-Tropsch process
  • the Fischer-Tropsch derived hydrocarbon product is suitably liquid at 0 0 C. If the product is not liquid it is preferably kept in the Above Ground Storage Tank at conditions at which the product is liquid.
  • the Fischer-Tropsch derived product can be the wax as is directly prepared in the Fischer-Tropsch synthesis step. Suitably this Fischer-Tropsch synthesis product is first subjected to a mild hydroisomerisation to reduce the congealing point of the product and increase its pumpability and to more easily have the product in the liquid state in the process of the present invention. Such a product is also referred to as Syncrude .
  • the Fischer-Tropsch derived hydrocarbon product may also be the lower boiling liquid fractions as isolated from the waxy Fischer-Tropsch product boiling between 35 and 300 0 C. These products comprising substantially, i.e. more than 80 wt%, of normal paraffins, may be shipped as hydrocarbon solvents, as steam cracker feedstock or as feedstock for the preparation of detergents.
  • the waxy product is subjected to a hydrocracking/hydroisomerisation process wherein lower boiling fractions are obtained, such as for example paraffin products boiling in the naphtha, kerosene and gas oil boiling range.
  • the partly isomerised liquid products so obtained may be shipped to end customers for use as aviation fuel, diesel fuel, industrial gas oil, drilling fluids, steam cracker feedstock or solvents.
  • the partly isomerised wax, also referred to as waxy raffinate, as obtained in such process steps may advantageously be further processed by means of solvent or catalytic dewaxing to obtain lubricating base oils or may be shipped as such to be used as an intermediate product to base oil manufacturing locations nearer to the end users.
  • Waxy raffinate is a distillate fraction.
  • Residual fractions boiling in the base oil range may also be used. However, it may be more difficult to keep these products in a liquid state during blending. Examples of such processes are described in more detail in US-A-6309432, US-A-6296757, US-A-5689031, EP-A-0668342, EP-A-0583836, US-A-6420618, WO-A-02/070631, WO-A-02/070629, WO-A-02/070627, WO-A-02/064710 and WO-A-02/070630.
  • the referred to hydrocracking/hydroisomerisation and optimal dewaxing steps are thus performed at the Fischer-Tropsch manufacturing location and the resulting above described liquid products are suited as the Fischer-Tropsch hydrocarbon products to be shipped.
  • the volume ratio between the mineral derived hydrocarbon product and the Fischer-Tropsch derived product may range, for example, from 1:99 to 99:1 and more preferably from 10:90 to 90:10.
  • the mineral derived hydrocarbon product preferably has a T90 vol% boiling point, as measured by ASTM D86, which is greater than the T50 vol% boiling point of the Fischer-Tropsch derived hydrocarbon product. More preferably, more than 50vol%, and even more preferably more than 80 vol%, of the boiling ranges of the mineral and the Fischer-Tropsch derived products overlap.
  • the mineral hydrocarbon product may be any product which is extracted from a subterranean environment or derivatives therefrom.
  • Examples of such products are crude mineral oil, gas field condensates, plant condensates, naphtha, kerosene, gas oil, vacuum distillates, deasphalted oils and residual fractions of crude oils.
  • Examples of combinations for which the present process will find utility are the blending of mineral crude oil and syncrude, blending of Fischer-Tropsch derived naphtha and gas field condensate, blending of Fischer-Tropsch derived gas oil and mineral derived gas oil and the blending of Fischer-Tropsch derived waxy raffinate and mineral oil derived vacuum distillates and/or mineral oil derived deasphalted oil.
  • the Fischer-Tropsch derived hydrocarbon product is the gas oil fraction, preferably as obtained after hydroisomerisation .
  • the gas oil product may thus be obtained by fractionation of such a Fischer-Tropsch synthesis product or obtained from a hydroconverted (hydrocracking/hydroisomerisation) Fischer-Tropsch synthesis product.
  • the gas oil may have been subjected to a catalytic dewaxing treatment. Mixtures of the afore mentioned gas oil fractions may also be used as the Fischer-Tropsch derived hydrocarbon product.
  • Fischer-Tropsch derived gas oils are described in EP-A-0583836, WO-A-97/14768, WO-A-97/14769, WO-A-00/11116, WO-A-00/11117, WO-A-01/83406 , WO-A-01/83648, WO-A-01/83647, WO-A-01/83641, WO-A-00/20535, WO-A-00/20534, EP-A-1101813, WO-A-03/070857 and US-A-6204426.
  • the Fischer-Tropsch derived gas oil will consist of at least 90 wt%, more preferably at least 95 wt% of iso and linear paraffins.
  • the weight ratio of iso-paraffins to normal paraffins will suitably be greater than 0.3. This ratio may be up to 12. Suitably this ratio is from 2 to 6. The actual value for this ratio will be determined, in part, by the hydroconversion process used to prepare the Fischer-Tropsch derived gas oil from the Fischer-Tropsch synthesis product. Some cyclic-paraffins may be present. By virtue of the Fischer-Tropsch process, the Fischer-Tropsch derived gas oil has essentially zero content of sulphur and nitrogen (or amounts which are no longer detectable) . These heteroatom compounds are poisons for Fischer-Tropsch catalysts and are removed from the synthesis gas that is the feed for the Fischer-Tropsch process.
  • the process does not make aromatics, or, as usually operated, virtually no aromatics are produced.
  • the content of aromatics as determined by ASTM D 4629 will typically be below 1 wt%, preferably below 0.5 wt% and most preferably below 0.1 wt%.
  • the Fischer-Tropsch derived gas oil will suitably have a distillation curve which will for its majority be within the typical gas oil range: from 150 to 400 0 C.
  • the Fischer-Tropsch gas oil will suitably have a T90 wt% of from 320 to 400 0 C, a density of from 0.76 to 0.79 g/cm 3 at 15°C, a cetane number greater than 70, suitably from 74 to 82, and a viscosity of from 1.9 to 4.5 centistokes at 40 0 C.
  • the above Fischer-Tropsch derived gas oil is preferably blended with a mineral derived kerosene or gas oil or mixtures of said kerosene and gas oil.
  • Preferred mineral derived gas oils or kerosenes are gas oils or kerosenes as obtained from refining and optionally
  • the mineral derived gas oil may be a single gas oil stream as obtained in such a refinery process or be a blend of several gas oil fractions obtained in the refinery process via different processing routes.
  • Examples of such different gas oil fractions as produced in a refinery are straight run gas oil, vacuum gas oil, gas oil as obtained in a thermal cracking process and light and heavy cycle oil as obtained in a fluid catalytic cracking unit and gas oil as obtained from a hydrocracker unit or the equivalent kerosene fraction.
  • the straight run gas oil or kerosene fraction is the fraction which has been obtained in the atmospheric distillation of the crude mineral refinery feedstock.
  • the above fractions suitably have an Initial Boiling Point (IBP) of from 150 to 280 0 C and a Final Boiling
  • IBP Initial Boiling Point
  • the vacuum gas oil is the gas oil fraction as obtained in the vacuum distillation of the residue as obtained in the above referred to atmospheric distillation of the crude mineral refinery feedstock.
  • the vacuum gas oil has an IBP of from 240 to 300 0 C and a FBP of from 340 to 380 0 C.
  • the thermal cracking process also produces a gas oil fraction, which may be used in step (a) .
  • This gas oil fraction has an IBP of from 180 to 28O 0 C and a FBP of from 320 to 380 0 C.
  • the light cycle oil fraction as obtained in a fluid catalytic cracking process will have an IBP of from 180 to 260 0 C and a FBP of from 320 to 380 0 C.
  • the heavy cycle oil fraction as obtained in a fluid catalytic cracking process will have an IBP of from 240 to 280 0 C and a FBP of from 340 to 38O 0 C.
  • These feedstocks may have a sulphur content of above 0.05 wt%.
  • the maximum sulphur content will be about 2 wt%.
  • the Fischer-Tropsch derived gas oil comprises almost no sulphur it could still be necessary to lower the sulphur level of the mineral derived gas oil in order to meet the current stringent low sulphur specifications.
  • the reduction of sulphur will be performed by processing these gas oil fractions in a hydrodesulphurisation (HDS) unit.
  • HDS hydrodesulphurisation
  • Gas oil as obtained in a fuels hydrocracker has suitably an IBP of from 150 to 28O 0 C and a FBP of from 320 to 380 0 C.
  • the cetane number of the blend of mineral derived gas oil as described above is preferably greater than 40 and less than 70. If also other properties like, for example, cloud point, CFPP (cold filter plugging point), flash point, density, di+-aromatics content, polyaromatics and/or distillation temperature for 95% recovery comply with the local regulations, the blend may be advantageously used as a diesel fuel component.
  • the final blended gas oil product comprising the Fischer-Tropsch and the mineral derived gas oil will have a sulphur content of at most 2000 ppmw (parts per million by weight) sulphur, preferably no more than 500 ppmw, most preferably no more than 50 or even 10 ppmw.
  • the density of such a blend is typically less than 0.86 g/cm ⁇ at 15°C, and preferably less than
  • the lower density of such a blend as compared to conventional gas oil blends results from the relatively low density of the Fischer-Tropsch derived gas oils .
  • the above fuel composition is suited as fuel in an indirect injection diesel engine or a direct injection diesel engine, for example of the rotary pump, in-line pump, unit pump, electronic unit injector or common rail type.
  • the final gas oil blend may be an additised (additive-containing) oil or an unadditised
  • additive-free oil If the fuel oil is an additised oil, it will contain minor amounts of one or more additives .
  • Detergent-containing fuel additives are known and commercially available. Such additives may be added to fuels at levels intended to reduce, remove or slow the build up of engine deposits.
  • detergents suitable for use in fuel additives for the present purpose include polyolefin substituted succinimides or succinamides of polyamines, for instance polyisobutylene succinimides or polyisobutylene amine succinamides, aliphatic amines, Mannich bases or amines and polyolefin (e.g. polyisobutylene) maleic anhydrides.
  • Succinimide dispersant additives are described for example in GB-A-960493, EP-A-0147240, EP-A-0482253, EP-A-0613938, EP-A-0557516 and WO-A-98/42808.
  • Particularly preferred are polyolefin substituted succinimides such as polyisobutylene succinimides.
  • additive components include lubricity enhancers, including ester- and acid-based additives; dehazers, e.g. alkoxylated phenol formaldehyde polymers; anti-foaming agents (e.g. polyether-modified polysiloxanes ) ; ignition improvers (cetane improvers) (e.g. 2-ethylhexyl nitrate (EHN), cyclohexyl nitrate, di-tert-butyl peroxide and those disclosed in US-A-4208190 at column 2, line 27 to column 3, line 21); anti-rust agents (e.g.
  • succinic acid derivative having on at least one of its alpha-carbon atoms an unsubstituted or substituted aliphatic hydrocarbon group containing from 20 to 500 carbon atoms, e.g. the pentaerythritol diester of polyisobutylene- substituted succinic acid); corrosion inhibitors; reodorants; anti-wear additives; anti-oxidants (e.g.
  • phenolics such as 2, 6-di-tert-butylphenol, or phenylenediamines such as N, N ' -di-sec-butyl-p- phenylenediamine) ; metal deactivators; and combustion improvers .
  • the additive concentration of each such additional component in the additivated fuel composition is preferably up to 1 %w/w, more preferably in the range from 5 to 1000 ppmw, advantageously from 75 to 300 ppmw, such as from 95 to 150 ppmw.
  • an oxygenate type fuel component may be present in the final blend to obtain diesel fuel as for example described in WO-A-2004/035713.
  • the oxygenate fuel may be present in a content of from 2 to 20 wt%, more preferably from 2 to 10 wt% as measured in the final fuel composition.
  • It preferably contains from 1 to 18 carbon atoms and in certain cases from 1 to 10 carbon atoms. Ideally it is biodegradable. It is suitably derived from organic material, as in the case of currently available ⁇ “biofuels” such as vegetable oils and their derivatives.
  • Preferred oxygenates for use are esters, for example alkyl, preferably C 1 to Cg or C ] _ to C5, such as methyl or ethyl, esters of carboxylic acids of vegetable oils.
  • the carboxylic acid in this case may be an optionally substituted, straight or branched chain, mono-, di- or multi-functional C 1 to C5 carboxylic acid, typical substituents including hydroxy, carbonyl, ether and ester groups.
  • Suitable examples of oxygenates (iii) include succinates and levulinates.
  • Ethers are also usable as the oxygenate (iii), for example dialkyl (typically C 1 to C5) ethers such as dibutyl ether and dimethyl ether.
  • the oxygenate may be an alcohol, which may be primary, secondary or tertiary. It may in particular be an optionally substituted (though preferably unsubstituted) straight or branched chain C ] _ to Cg alcohol, suitable examples being methanol, ethanol, n-propanol and iso-propanol .
  • Typical substituents include carbonyl, ether and ester groups. Methanol and in particular ethanol may for instance be used.
  • the oxygenate (iii) will typically be a liquid at ambient temperature, with a boiling point preferably from 100 to 360°C, more preferably from 250 to 290°C. Its density is suitably from 0.75 to 1.2 g/cm 3 , more preferably from 0.75 to 0.9 g/cm 3 at 15° C (ASTM D4502 / IP 365), and its flash point greater than 55 °C. Adding the additives and/or the oxygenates may be performed during the process of the present invention. Even more preferred is to add at least part of the additives and/or the oxygenates when discharging the blended product from the storage vessel. Addition is preferably performed by means of so-called in-line blending.
  • the blend as thus obtained can be directly used as a finished fuel for use as Automotive Gas Oil (AGO) or as an Industrial Gas Oil (IGO) .
  • AGO Automotive Gas Oil
  • IGO Industrial Gas Oil
  • substantially above in the sense of the process of the present invention is meant that at least 50, preferably at least 70 and even more preferably at least 90 vol%, of the Fischer-Tropsch derived product is present in the lower half of the Above Ground Storage Tank.
  • the mineral hydrocarbon product is preferably supplied first and the Fischer-Tropsch derived product second.
  • a “blended product” is meant a mixture wherein the difference in density between a sample taken at 10% of the liquid height below the liquid surface, referred to as dlO, and the density of a sample taken at 90% of the liquid height below the liquid surface, referred to as d90, is small, preferably such that the ratio of the (dl0-d90 ) /dlO is less than 0.01, more preferably less than 0.001.
  • the "Above Ground Storage Tank” also referred to as a "AST" in the sense of the present invention is a storage facility fixed to the surface of the earth.
  • the Above Ground Storage Tank is part of a so-called blending facility or tanker park.
  • the Above Ground Storage Tank has suitably a storage volume of greater than 3000 m 3 , more preferably greater than 10000 m3.
  • the upper limit of the storage facility of a single Above Ground Storage Tank is suitably 100000 m 3 .
  • the Above Ground Storage Tank may be equipped with additional mixing devices as may be present in Above Ground Storage Tanks. An advantage of the process of the present invention is that such devices may be omitted or used at a lower rate.
  • the present invention is also directed to a blended product produced by the process to blend according to the present invention.
  • the present invention is further directed to the direct use of the blended product as a fuel, more preferably as an automotive gas oil or as an industrial gas oil, as obtained by the process of the present invention.
  • Example 1 The present invention will be illustrated by means of the following non-limiting examples .
  • Example 2 The present invention will be illustrated by means of the following non-limiting examples .
  • a typical mineral derived gas oil (further referred to as AGO) and a typical Fischer-Tropsch gas oil (further referred to as GTL) having the properties as listed in Table 1 were used in the following experiment.
  • AGO mineral derived gas oil
  • GTL Fischer-Tropsch gas oil
  • each technique was to minimise turbulence (and hence mixing) during addition of the second fuel so that the majority of any mixing of the two fuels was due to the length of the contact time.
  • Both techniques involved the preparation of 2 x 2 litre glass beakers, one containing 800 ml of AGO, the other containing 800 ml of GTL. To the AGO, 800 ml of GTL was added slowly, using a 1 litre glass cylinder, taking approximately 2 minutes to complete (Blend A.) This technique was repeated for the addition of the AGO (800 ml) to GTL (Blend B) .
  • densities of the fuel blends were measured after a period of time at 400 ml and 1200 ml from the bottom of the beaker to assess the density at bottom and top of each blend.
  • the funnel technique for fuel addition involved the pouring of the added fuel over the outer surface of an upside down glass funnel that had its base (funnel mouth) in contact with the inner walls of the glass beaker. This was designed to produce fuel addition over a large surface area, minimise turbulence and hence minimise the mixing of the two fuel layers during addition of the second fuel.
  • the beaker technique for fuel addition involved the direct pouring of the added fuel down the inner wall of the beaker. This produced fuel addition over a smaller surface area than that of the funnel technique, more turbulence and hence more mixing of the two fuel layers during addition of the second fuel.
  • Density follows, volume/volume, linear blending rules and a homogeneous 50:50 blend of the AGO and GTL samples studied will have a theoretical density of 813.3 kg/m ⁇ .
  • density measurements of the blends can be used to calculate the amount of each component present.
  • Table 2 depicts the density results and calculated percentage for each component sampled at a depth represented by a volume of 400 ml (bottom) , and 1200 ml (top) on the graduated beaker. It should be noted that the density result of 841.8 kg/m ⁇ obtained for Blend A 'Bottom' - funnel method, is greater than 841.4 kg/m ⁇ - the density of neat AGO.

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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)
  • Liquid Carbonaceous Fuels (AREA)
  • Lubricants (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L’invention concerne un procédé de mélange d’un produit hydrocarboné dérivé d’un minéral et d’un produit hydrocarboné dérivé de Fischer-Tropsch, ledit procédé consistant à introduire dans un réservoir de stockage de surface une quantité d’un produit hydrocarboné dérivé d’un minéral et d’un produit hydrocarboné dérivé de Fischer-Tropsch, de manière à ce que le produit hydrocarboné dérivé d’un minéral soit initialement situé essentiellement au dessus du produit hydrocarboné dérivé de Fischer-Tropsch ; un produit mélangé obtenu par le procédé ; et l’utilisation du produit mélangé.
EP20060793664 2005-09-21 2006-09-20 Procede de melange d' un produit hydrocarbone derive d' un mineral et d' un produit hydrocarbone derive de fisher-tropsch Ceased EP1926802A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20060793664 EP1926802A1 (fr) 2005-09-21 2006-09-20 Procede de melange d' un produit hydrocarbone derive d' un mineral et d' un produit hydrocarbone derive de fisher-tropsch

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP05108729 2005-09-21
EP20060793664 EP1926802A1 (fr) 2005-09-21 2006-09-20 Procede de melange d' un produit hydrocarbone derive d' un mineral et d' un produit hydrocarbone derive de fisher-tropsch
PCT/EP2006/066533 WO2007039460A1 (fr) 2005-09-21 2006-09-20 Procede de melange d’un produit hydrocarbone derive d’un mineral et d’un produit hydrocarbone derive de fisher-tropsch

Publications (1)

Publication Number Publication Date
EP1926802A1 true EP1926802A1 (fr) 2008-06-04

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Country Link
US (1) US20070135664A1 (fr)
EP (1) EP1926802A1 (fr)
JP (1) JP5281404B2 (fr)
CN (1) CN101305080A (fr)
AU (1) AU2006298850A1 (fr)
BR (1) BRPI0616281A2 (fr)
WO (1) WO2007039460A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2909097B1 (fr) * 2006-11-27 2012-09-21 Inst Francais Du Petrole Procede de conversion de gaz en liquides a logistique simplifiee
BRPI0819886A2 (pt) * 2007-12-07 2015-06-16 Shell Int Research Formulação de óleo de base, uso de um óleo de base leve derivado de fischer-tropsch, e, métodos para melhorar uma propriedade de uma formação de óleo de base e para preparar uma formulação de óleo de base
WO2018077976A1 (fr) * 2016-10-27 2018-05-03 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'un gazole automobile
WO2018206729A1 (fr) * 2017-05-11 2018-11-15 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'une fraction de gazole automobile

Family Cites Families (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1101813A (en) * 1913-08-28 1914-06-30 Champion Machine & Forging Company Process of forging.
JPS59187575A (ja) * 1983-03-11 1984-10-24 東亜燃料工業株式会社 原油タンク
US5059299A (en) * 1987-12-18 1991-10-22 Exxon Research And Engineering Company Method for isomerizing wax to lube base oils
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)
US5147418A (en) * 1991-12-19 1992-09-15 Chicago Bridge & Iron Technical Services Company Volatile liquid storage system
US6296757B1 (en) * 1995-10-17 2001-10-02 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US5689031A (en) * 1995-10-17 1997-11-18 Exxon Research & Engineering Company Synthetic diesel fuel and process for its production
US5766274A (en) * 1997-02-07 1998-06-16 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US6162956A (en) * 1998-08-18 2000-12-19 Exxon Research And Engineering Co Stability Fischer-Tropsch diesel fuel and a process for its production
US6080301A (en) * 1998-09-04 2000-06-27 Exxonmobil Research And Engineering Company Premium synthetic lubricant base stock having at least 95% non-cyclic isoparaffins
US6204426B1 (en) * 1999-12-29 2001-03-20 Chevron U.S.A. Inc. Process for producing a highly paraffinic diesel fuel having a high iso-paraffin to normal paraffin mole ratio
US6663767B1 (en) * 2000-05-02 2003-12-16 Exxonmobil Research And Engineering Company Low sulfur, low emission blends of fischer-tropsch and conventional diesel fuels
WO2001083648A2 (fr) * 2000-05-02 2001-11-08 Exxonmobil Research And Engineering Company Melanges a faibles emissions constitues de carburant f-t/matiere premiere de craquage
JP2002120900A (ja) * 2000-10-16 2002-04-23 Ishikawajima Harima Heavy Ind Co Ltd 密度の異なる液体を貯槽へ混合充填する方法及び液化窒素と液化酸素を液化貯槽へ混合充填する方法
US6541524B2 (en) * 2000-11-08 2003-04-01 Chevron U.S.A. Inc. Method for transporting Fischer-Tropsch products
US6518321B1 (en) * 2000-11-08 2003-02-11 Chevron U.S.A. Inc. Method for transporting Fischer-Tropsch products
US6806237B2 (en) * 2001-09-27 2004-10-19 Chevron U.S.A. Inc. Lube base oils with improved stability
AU2003229676A1 (en) 2002-04-15 2003-10-27 Shell Internationale Research Maatschappij B.V. Method to increase the cetane number of gas oil
ITMI20021131A1 (it) * 2002-05-24 2003-11-24 Agip Petroli Composizioni essenzialmente idrocarburiche utilizzabili come carburanti con migliorate proprieta' lubrificante
US7144497B2 (en) * 2002-11-20 2006-12-05 Chevron U.S.A. Inc. Blending of low viscosity Fischer-Tropsch base oils with conventional base oils to produce high quality lubricating base oils
EP1627028B1 (fr) * 2003-05-22 2007-12-12 Shell Internationale Research Maatschappij B.V. Procede d'amelioration de coupes gazoles et kerosenes de petrole brut
US7087804B2 (en) * 2003-06-19 2006-08-08 Chevron U.S.A. Inc. Use of waste nitrogen from air separation units for blanketing cargo and ballast tanks
US7479216B2 (en) * 2004-09-28 2009-01-20 Chevron U.S.A. Inc. Fischer-Tropsch wax composition and method of transport
US7488411B2 (en) * 2004-09-28 2009-02-10 Chevron U.S.A. Inc. Fischer-tropsch wax composition and method of transport
US20060065573A1 (en) * 2004-09-28 2006-03-30 Chevron U.S.A. Inc. Fischer-tropsch wax composition and method of transport

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
K SHAINE TYSON: "BIODIESEL Handling and use guidelines", 1 September 2001 (2001-09-01), XP055186737, Retrieved from the Internet <URL:http://www.biofuels.coop/archive/HandlingAndUse2001.pdf> [retrieved on 20150429] *
See also references of WO2007039460A1 *

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JP5281404B2 (ja) 2013-09-04
JP2009509020A (ja) 2009-03-05
CN101305080A (zh) 2008-11-12
AU2006298850A1 (en) 2007-04-12
US20070135664A1 (en) 2007-06-14
BRPI0616281A2 (pt) 2016-08-23

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