CN102510893A - Fuel production from feedstock containing triglyceride and/or fatty acid alkyl ester - Google Patents

Fuel production from feedstock containing triglyceride and/or fatty acid alkyl ester Download PDF

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Publication number
CN102510893A
CN102510893A CN2010800420525A CN201080042052A CN102510893A CN 102510893 A CN102510893 A CN 102510893A CN 2010800420525 A CN2010800420525 A CN 2010800420525A CN 201080042052 A CN201080042052 A CN 201080042052A CN 102510893 A CN102510893 A CN 102510893A
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CN
China
Prior art keywords
weight
raw material
fuel
lipid
oil
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CN2010800420525A
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Chinese (zh)
Inventor
帕特里克·L·汉克斯
威廉姆·J·诺瓦克
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ExxonMobil Technology and Engineering Co
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ExxonMobil Research and Engineering Co
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Publication of CN102510893A publication Critical patent/CN102510893A/en
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    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
    • C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
    • C10G3/49—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, e.g. molecular sieves
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/12—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1018—Biomass of animal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1051—Kerosene having a boiling range of about 180 - 230 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Abstract

This invention relates to processes for the production of a fuel composition from a feedstock that comprises lipid material (e.g., bio- material) and mineral oil. The processes can be carried out without producing a significant mount of undesirable side reactions such as cracking, polymerization, and aromatization, which can be an undesirable consequence of large heats of reaction. As a result, the invention provides for the production of a product that is relatively high in quality, and catalyst used in the processes is not adversely affected to any significant extent.

Description

From containing the raw material production fuel of tri-glyceride and/or fatty acid alkyl ester
Technical field
The present invention relates to from comprising the raw material production fuel composition of lipid material and MO.More specifically, the present invention relates to from comprising MO and at least a transport fuel compsn of raw material production that is selected from the lipid material of tri-glyceride, fatty acid alkyl ester and combination thereof, wherein said production comprises at least one hydrocracking step.
Background technology
Because various environment and energy Consideration are in the manufacturing of fuel product, particularly transport fuel, promoting the use of biomaterial to have very big interest.In the manufacturing of fuel, interested field is through the vegetables oil that contains fatty acid triglyceride and the suitable diesel oil fuel of process for producing of animal tallow.
With vegetables oil or other derivative of fatty acid be transformed into fuel for example the standard method of diesel oil kind of fuel be achieved through transesterification reaction.This reaction is included in catalyzer for example makes vegetables oil contact with methyl alcohol under the sodium hydroxide existence.The product that produces is a fatty acid methyl ester, and this product can directly be used as the blending component of diesel oil fuel or diesel oil fuel.
Yet the fuel product that forms from simple ester-exchange reaction is with various fuel mass problems.In these problems some comprise that cold flow properties difference and oxidative stability are low.
Hydrotreatment be for overcome with from some relevant problems of fuel of the raw material production of vegetables oil type and a kind of treatment type that proposes.For example, U.S. Patent application discloses 2009/0166256 to disclose sulphur content low and comprise the method for manufacture up to the diesel boiling range hydro carbons of 20 weight % biological components raw materials.Said method comprises uses the hierarchical common hydroprocessing process, makes the diesel boiling range hydro carbons from least a biological components raw material and at least a mineral hydrocarbon raw material.
Still be used for producing other method of high quality fuel from biomaterial in searching.Specifically, searching can be produced various transport fuels, comprises the method for gasoline, kerosene, rocket(engine)fuel and diesel oil.In addition, hope that very said method can rationally control undesirable side reaction when carrying out.Undesirable side reaction can not only cause fuel mass to reduce, and the catalyzer that uses in the reaction process is also had disadvantageous effect.
Summary of the invention
The invention provides and be used for from the biomaterial method of lipid material produce fuel, particularly transport fuel for example.Product comprises one or more high quality transport fuels, for example gasoline, kerosene, rocket(engine)fuel and diesel oil fuel.
The method of production and transport fuel is provided according to an aspect of the present invention.Said method comprises produces or provides the raw material that contains lipid material and MO.Preferably, said lipid material can be selected from tri-glyceride, fatty acid alkyl ester and combination thereof.Said raw material can be by hydrogen cracking to produce transport fuel.
According to a further aspect in the invention; The method of production and transport fuel is provided; Said method comprises preparation or the step of supplying raw materials; Said raw material contains the MO that is no more than 99 weight % based on the gross weight content of said raw material, and the lipid material that is selected from tri-glyceride, fatty acid alkyl ester and combination thereof.Preferably, said raw material can have at least 100 ℃ initial boiling point and/or be no more than 500 ℃ full boiling point.Said raw material can be by hydrogen cracking to produce transport fuel.
Embodiment
The invention provides and be used for from comprising the for example method of raw material production one or more high quality fuel, particularly at least a transport fuel of lipid or lipid material of biomaterial.Can carry out said method and do not produce for example cracking of undesirable side reaction, polymerization and the aromizing of significant quantity, it possibly be the result of a large amount of reaction heat.Therefore, the invention provides the production of high quality product.In addition, the catalyzer that in said method, uses does not receive the disadvantageous effect of any significance degree.
The raw material that uses in the present invention comprises lipid material and MO." MO " is meant fossil/mineral fuel for example crude oil of originating, be not the commercialization organic products for example by Aldrich at the CAS numbering 8020-83-5 organic products of sale down.In one embodiment, before processing, lipid material and mineral oil are in the same place.In another embodiment, lipid material and MO are provided in the suitable treatment unit or container as the materials flow that separates.
Term used according to the invention " lipid material " is the compsn that comprises biomaterial.Usually, these biomaterials comprise vegetation fat/oil, animal tallow/oil, fish oil, cracked oil and algae lipid/oils, and the component of these materials.More specifically, said lipid material comprises the lipoid substance of one or more types.Lipoid substance is generally water insoluble but is dissolved in the biological compound of nonpolar (or fat) solvent.The limiting examples of such solvent comprises alcohol, ether, chloroform, alkyl acetate, benzene and combination thereof.
The main type of lipid comprise but must not be limited to lipid acid, come from glycerine lipid (comprising fat, oil and phosphatide), come from lipid (comprising ceramide type, cerebroside, gangliosides and sphingomyelin class), steroid class and verivate, terpenes and verivate thereof, liposoluble vitamin, some aromatic substance and the long-chain alcohol and the wax of sphingosine.
In live organism, lipid generally is used as the principal constituent of cytolemma and is used as the form of fuel storage.Lipid also can exist with protein or carbohydrate coupling, for example with the form of lipoprotein and LPS.
The instance that can be used for vegetables oil of the present invention includes but not limited to vegetable seed (mustard seed) oil, VT 18, Oleum Cocois, Trisun Oil R 80, plam oil, palm-kernel oil, peanut oil, linseed oil, Yatall MA, Semen Maydis oil, Viscotrol C, curcas oil, Jojoba oil, sweet oil, Semen Lini oil, false flax oil, Thistle oil, babassu benevolence oil, tallow oil and Rice pollard oil.
The vegetables oil of here mentioning also can comprise finished vegetables oil material.The limiting examples of finished vegetables oil material comprises lipid acid and fatty acid alkyl ester.Alkyl ester generally includes C 1-C 5Alkyl ester.Be preferably in methyl, ethyl and the propyl diester one or more.
The instance that can be used for animal tallow of the present invention includes but not limited to beef fat (tallow), lard (lard), turkey fat, fish tallow/oil and chicken fat.Said animal tallow can comprise that dining room and meat production factory obtain from any suitable source.
The animal tallow of here mentioning also comprises finished animal tallow material.The limiting examples of finished animal tallow material comprises lipid acid and fatty acid alkyl ester.Alkyl ester generally includes C 1-C 5Alkyl ester.Be preferably in methyl, ethyl and the propyl diester one or more.
Algae oil or lipid are included in the algae with the form of membrane component, stored product and metabolite usually.Some algae strain, particularly little algae be diatom and blue-green algae for example, contains a high proportion of lipid levels.Be used for the alga-derived of algae oil, the gross weight based on himself biomass can contain the for example lipids of 2 weight % to 40 weight % of different amounts.
Being used for the alga-derived of algae oil includes but not limited to unicellular and the many cells algae.The instance of such algae comprises rhodophyta, Chlorophyta, not isometric flagellum door, tribophyte, grey born of the same parents algae door, filopodium worm door (chlorarachniophyte), Euglena, decides the whip algae, conceals algae, dinoflagellate, plant plankton etc. and combination thereof.In one embodiment, algae can be the algae of Chlorophyceae and/or Haptophyceae.Concrete species can include but not limited to the new green alga of rich oil (Neochloris oleoabundans), dimorphism grid algae (Scenedesmus dimorphus), very thin Euglena (Euglena gracilis), Phaeodactylum tricornutum (Phaeodactylum tricornutum), cocolith (Pleurochrysis carterae), decide whip algae (Prymnesium parvum), flat algae (Tetraselmis chui) and Chlamydomonas reinhardtii (Chlamydomonas reinhardtii) for a short time.
The lipid material part of said raw material can comprise tri-glyceride, fatty acid alkyl ester or preferably its combination.In one embodiment; Be processed into the gross weight of the raw material of fuel based on being used to of being provided; Said raw material can comprise the lipid material of at least 0.05 weight %, preferred at least 0.5 weight %, the lipid material of at least 1 weight %, at least 2 weight % or at least 4 weight % for example.
In addition or alternatively, based on the gross weight of said raw material, said raw material can comprise the lipid material that is no more than 40 weight %, preferably be no more than 30 weight %, for example be no more than 20 weight % or be no more than the lipid material of 10 weight %.
In one embodiment, said lipid material comprises tri-glyceride.The type of tri-glyceride can be confirmed according to their fatty acid component.Can use gc (GC) analysis easily to measure said fatty acid component.This analysis comprises extraction fat or oily, and fat or oil are carried out saponification (hydrolysis), the fat or oily alkyl (for example methyl) ester of preparation saponification, and use GC to analyze the type of confirming (methyl) ester.In one embodiment, based on the total tri-glyceride that exists in the said lipid material, the major part of the tri-glyceride that exists in the said lipid material (promptly surpassing 50%) can be by C 8To C 22Fatty acid component constitutes.For the sake of clarity, be called as " C when lipid acid or fatty ester molecule Xx" when lipid acid, fatty acid component or fatty ester, it means that " xx " connects the carbon number on carbon one side of key at carboxylicesters, promptly comprise carboxylicesters carbon, and in fatty ester, ester carbon is not included in " C Xx" in and be that carboxylicesters connects the carbon on oxygen one side of key, promptly end at carboxylicesters oxygen.In addition, tri-glyceride is the molecule that has same structure with the reaction product of glycerine and three lipid acid.Therefore, constitute although tri-glyceride is described as by lipid acid in this article, should be appreciated that, said fatty acid component must not contain carboxylic acid hydrogen.In the method for the invention, based on the total tri-glyceride that exists in the said lipid material, the most of tri-glyceride that exists in the said lipid material preferably can be by C 10To C 18, for example C 12To C 18Fatty acid component constitutes.
In specific implementations, said lipid material comprises tri-glyceride, wherein at least 20 weight %, preferred at least 30 weight %, for example the tri-glyceride of at least 40 weight % is made up of LAURIC ACID 99 MIN (C 12:0) composition.Use representation " C xx:yy " expression compound on the main chain, be to comprise that carboxylicesters carbon has " xx " individual carbon on carboxylate group's carbon one side, and on this main chain, have " yy " individual pair of key.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 40 weight % to 60 weight %, for example the tri-glyceride of 42 weight % to 58 weight % or 44 weight % to 55 weight % is made up of the LAURIC ACID 99 MIN composition.Only if clearly indicate in addition, otherwise the percentage ratio of explaining among this paper is based on the percentage ratio of the total amount of multiple key element or composition.
In addition or alternatively, said lipid material comprises tri-glyceride, wherein at least 2 weight %, preferred at least 5 weight %, for example the tri-glyceride of at least 10 weight % is made up of tetradecanoic acid (C 14:0) composition.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 10 weight % to 28 weight %, for example the tri-glyceride of 12 weight % to 26 weight % or 14 weight % to 24 weight % is made up of the tetradecanoic acid composition.
In addition or alternatively, said lipid material comprises tri-glyceride, wherein at least 2 weight %, preferred at least 3 weight %, for example the tri-glyceride of at least 5 weight % is made up of palmitinic acid (C16:0) composition.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 2 weight % to 12 weight %, for example the tri-glyceride of 3 weight % to 10 weight % or 5 weight % to 8 weight % is made up of the palmitinic acid composition.
In addition or alternatively, said lipid material comprises tri-glyceride, wherein at least 0.5 weight %, preferred at least 1 weight %, for example the tri-glyceride of at least 2 weight % is made up of Triple Pressed Stearic Acid (C18:0) composition.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 0.5 weight % to 60 weight %, for example the tri-glyceride of 1 weight % to 55 weight % or 2 weight % to 50 weight % is made up of the Triple Pressed Stearic Acid composition.
In addition or alternatively, said lipid material comprises tri-glyceride, wherein at least 5 weight %, preferred at least 6 weight %, for example the tri-glyceride of at least 7 weight % is made up of oleic acid (C 18:1) composition.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 5 weight % to 30 weight %, for example the tri-glyceride of 6 weight % to 25 weight % or 7 weight % to 20 weight % is made up of the oleic acid composition.
In addition or alternatively, said lipid material comprises tri-glyceride, wherein at least 2 weight %, preferred at least 3 weight %, for example the tri-glyceride of at least 4 weight % is made up of sinapinic acid (C22:1) composition.In addition or alternatively, said lipid material comprises tri-glyceride, wherein 2 weight % to 70 weight %, for example the tri-glyceride of 3 weight % to 65 weight % or 4 weight % to 60 weight % is made up of the sinapinic acid composition.
In one embodiment, said lipid material comprises fatty acid alkyl ester.Preferably, said fatty acid alkyl ester comprises fatty acid methyl ester (FAME), fatty-acid ethyl ester (FAEE) and/or lipid acid propyl ester.
In particular of the present invention, the lipid material of said raw material partly comprises fatty acid alkyl ester, and the most of fatty acid alkyl ester that exists in the said lipid material is preferably FAME.
In another embodiment of the present invention, based on the gross weight of said lipid material, lipid material in said raw material part can comprise at least 20 weight %, preferred at least 30 weight %, the fatty acid alkyl ester of at least 40 weight % for example, preferred FAME.Preferably, most of fatty acid component of said fatty acid alkyl ester, preferred FAME can be selected from sad (C 8:0), capric acid (C 10:0), LAURIC ACID 99 MIN (C 12:0), tetradecanoic acid (C 14:0), palmitinic acid (C16:0), Zoomeric acid (C 16:1), Triple Pressed Stearic Acid (C 18:0), oleic acid (C 18:1), linolic acid (C 18:2), linolenic acid (C 18:3), sinapinic acid (C22:1) and combination thereof.In specific implementations; Based on the total amount of the FAME that exists in the said lipid material part, most of fatty acid component of the FAME that exists in the said lipid material part can be selected from LAURIC ACID 99 MIN (C12:0), tetradecanoic acid (C 14:0), palmitinic acid (C 16:0), Zoomeric acid (C 16:1), Triple Pressed Stearic Acid (C 18:0), oleic acid (C 18:1) and combination thereof.
Raw material provided by the present invention comprises MO.The instance of MO can include but not limited to straight run (normal pressure) gas oil; Vacuum gas oil; Metallization removal oil; Coker distillate; The catalytic cracking distilled oil; Heavy naphtha (choosing wantonly but preferably part denitrogenation and/or partial desulfurization at least at least); Diesel boiling range cut (choosing wantonly but preferably part denitrogenation and/or partial desulfurization at least at least); Rocket(engine)fuel boiling range cut (choosing wantonly but preferably part denitrogenation and/or partial desulfurization at least at least); Kerosene boiling range cut (choosing wantonly but preferably part denitrogenation and/or partial desulfurization at least at least) and coal slurry.As the involved MO of said part of raw materials, can comprise any or its any combination that is suitable in these example materials flows of said lipid material part hydrogen cracking.Preferably, said raw material does not contain any tangible asphaltene.In one embodiment, can said MO and said lipid material is partially mixed, carry out hydrotreatment then to form the material of hydrotreatment.In another embodiment, before partially mixed, can carry out hydrotreatment to reduce nitrogen and/or sulphur content to said MO with said lipid material.
Said MO component can contain nitrogenous compound (being called for short " nitrogen ").For example, based on the gross weight of said MO component, said MO can contain the nitrogen of 5wppm at least.Preferably, based on the gross weight of said MO component, said MO contains the nitrogen that is no more than 1.0 weight %.In general, most of the nitrogen will be the form of nitrogen-containing organic compound at least.
Said MO contains sulfocompound (being called for short " sulphur " or " sulphur content ") usually.Based on the gross weight of said MO, such compound is usually to be higher than 500wppm or to be present in the said MO usually above the sulphur content of 0.1 weight %.Preferably, based on the gross weight of said MO, the sulphur content of said MO is no more than 6 weight %, preferably is no more than 4 weight %.
In one embodiment, based on the gross weight of said raw material, said raw material can comprise the MO that is no more than 99 weight %.Preferably, based on the gross weight of said raw material, said raw material can comprise and is no more than 98 weight %, for example is no more than 95 weight %, is no more than 90 weight %, is no more than 85 weight % or is no more than the MO of 80 weight %.
In addition or alternatively, based on the gross weight of said raw material, said raw material can comprise the MO of at least 50 weight %.Preferably, based on the gross weight of said raw material, said raw material can comprise at least 60 weight %, for example the MO of at least 70 weight %, at least 75 weight % or at least 80 weight %.
According to an aspect of the present invention, the raw material that carries out hydrogen cracking can have at least 100 ℃, preferred at least 150 ℃, the for example initial boiling point of at least 180 ℃ or at least 200 ℃.The boiling point of the fuel composition of confirming these raw materials and producing according to the present invention or the fundamental test method of boiling range can be carried out through carrying out batch distillation according to " being used for petroleum products distillatory standard test methods under the normal atmosphere " (Standard Test Method for Distillation of Petroleum Products at Atmospheric Pressure) ASTM D86-09el.
In addition or alternatively, said raw material can have be no more than 500 ℃, preferably be no more than 450 ℃, for example be no more than 400 ℃ full boiling point.
Method of the present invention comprises carries out hydrogen cracking to produce the step of the fuel product of hoping to said raw material.Hydrogen cracking is meant resolves into than simple molecules some hydrocarbon molecules in the raw material that is provided to produce the process of fuel product.Common said fuel product can comprise one or more transport fuels, for example gasoline, kerosene, rocket(engine)fuel and/or diesel oil, and these discrete fuel can become its component portion through fractionation separates usually.
Can in the presence of hydrogen, choose wantonly but preferred contacting with hydrocracking catalyst through making said raw material, thereby carry out said hydrocracking process with the formation product.The cracking aspect of the process that is added to of hydrogen provides benefit; Because the common saturation ratio of fuel product that produces is higher; And can further reduce undesirable heteroatoms for example nitrogen, oxygen and sulphur, and also can advantageously reduce aromatic content and/or degree of unsaturation.
In one embodiment, the hydrocracking catalyst that in process of the present invention, uses can comprise amorphous base-material or zeolite base-material and one or more VIII families or group vib metal hydrogenation component.In another embodiment, said hydrocracking catalyst can comprise crystalline zeolite cracking base-material, deposits at least a VIII family or group vib metal hydrogenation component on it.Suitable VIII family and group vib metal can comprise cobalt, nickel, iron, molybdenum, tungsten and combination thereof.Except zeolite and/or amorphous base-material or alternative their appropriate carriers, can comprise the MOX of relative high-specific surface area, for example silicon-dioxide, silica-alumina, aluminum oxide and titanium oxide.Although comprising choosing wantonly, preferred implementation on carrier, comprises group vib metal and VIII family metal (for example with oxide form; Or preferably after curing under the cure conditions that said oxide form has been fit to) catalyzer; Said catalyzer can be in addition or is comprised other component alternatively; For example reagent such as other transition metal (for example V family metal for example niobium), rare earth metal, organic ligand (for example be added or as the precursor that stays after oxidation and/or the vulcanisation step), phosphorus compound, boron cpd, fluorochemicals, silicon-containing compound, promotor, sticker, weighting agent, or its combination.The family of mentioning in this article is meant the family of the CAS version that in the periodic table of elements among " the concise and to the point chemical dictionary of Hawley " (Hawley ' s Condensed Chemical Dictionary) the 13rd edition, exists.As explanation, suitable VIII/VIB family catalyzer is described in for example especially following one or more patents and the patented claim: USP 6,156,695,6,162; 350,6,299,760,6,582,590,6,712; 955,6,783,663,6,863,803,6,929; 738,7,229,548,7,288,182,7,410; 924 and 7,544,632, U.S. Patent application discloses 2005/0277545,2006/0060502,2007/0084754 and 2008/0132407, and International Publication WO 04/007646, WO2007/084437, WO 2007/084438, WO 2007/084439 and WO 2007/084471.
Can also can be called as molecular sieve as the zeolite as cracking base-material of hydrocracking catalyst component.These materials can by silicon-dioxide, aluminum oxide and one or more exchangeable cation for example sodium, magnesium, calcium and one or more other metals for example transition metal and/or rare earth metal constitute.
In an embodiment of the invention, can use the macropore crystalline molecular sieve.Preferably, said crystalline molecular sieve has and less than 2, for example is no more than 1 restricted index.The method of measuring restricted index is at USP 4,016, fully describes in 218, through with reference to being introduced among this paper.
In addition or alternatively, said hydrocracking catalyst can comprise the aperture and is at least 7 dusts, preferred at least 7.4 dusts, the molecular sieve of at least 8 dusts for example.Particularly preferably be by the aperture and be no more than the hydrocracking catalyst that the molecular sieve of 15 dusts constitutes.
The instance that can be used for the zeolite molecular sieve in the said hydrocracking catalyst includes but not limited to β zeolite, X zeolite, zeolite Y, faujusite, ultra steady Y (USY), dealuminzation Y (Deal Y), mordenite, ZSM-3, ZSM-4, ZSM-18, ZSM-20 etc., and combination.
In addition, preferred said hydrocracking catalyst has at least some acidity.Preferably, said hydrocracking catalyst have greater than 1, more preferably greater than 5, for example greater than 10 α value.The α value is the tolerance of zeolite acidity functionality, and compares the approximate indication of the catalytic cracking activity of catalyzer with standard catalyst.α value test has provided detecting catalyst and has been taken as 1 standard catalyst (rate constant=0.016 second with respect to the α value -1) relative rate constant (hexane conversion of time per unit per unit volume catalyzer).α value test description is at USP 3,354, and 078 and J.Catalysis:4,527 (1965); In several pieces of articles in 6,278 (1966) and 61,395 (1980), drawing with its description to said test at this is reference.The experiment condition that is used to measure the test of α value comprises about 538 ℃ steady temperature and variable flow rate, as at J.Catalysis, describes in detail in 61,395 (1980).The application of α value in acid zeolite is described in more detail in USP 4,016, in the article of the J.Catalysis magazine in 218 and 1966 years.
Said hydrocracking catalyst must not have peracidity, although can use the peracidity catalyzer.In one embodiment, said hydrocracking catalyst can have the α value that is no more than 200, for example is no more than 100.
Hydrogen cracking can be carried out under the condition of fuel product that effectively production hoped.In a preferred implementation, said hydrogen cracking can 300 ° of F (149 ℃) to 900 ° of F (482 ℃), be preferably 550 ° of F (289 ℃) and to the average reaction temperature of 800 ° of F (427 ℃), carry out.
In addition or alternatively, hydrogen cracking also can 400psia (27atm or 2.8MPaa) to 3000psia (200atm or 21MPaa), be preferably 500psia (34atm or 3.5MPaa) and to the average response pressure of 2000psia (140atm or 14MPaa), carry out.
In addition or alternatively, the hydrogen-containing treat gas speed in the hydrogen cracking can be at 300scf/ bucket (53Nm 3/ m 3) to 5000scf/ bucket (890Nm 3/ m 3), for example 2000scf/ bucket (360Nm 3/ m 3) to 4000scf/ bucket (710Nm 3/ m 3) scope in.
When mentioning in this manual; Handling gas can be pure hydrogen or hydrogen-containing gas; It contains the hydrogen of the amount of the reaction purpose that is enough to be used at least being planned; Optional in addition one or more other gases (for example nitrogen, light hydrocarbons methane etc. for example, and combination) that reaction or product do not had unfavorable interfere with or compromise that comprise in general.Impurity is H for example 2S and NH 3Usually undesirable, and usually before said processing gas is imported reactor drum with impurity from wherein removing.Being incorporated into processing gas stream in the step of reaction can preferably contain at least about 50 volume %, for example at least about the hydrogen of 75 volume %.
With volume/hour (V/V/Hr or Hr -1) liquid hourly space velocity in the hydrogen cracking of expression, usually 0.1 to 10, be preferably in 1 to 5 the scope.
Although these hydrocracking conditions mention in the embodiment that separates, imagined these hydrocracking reactions and can carry out two kinds of the disclosed reaction of this paper or above or even any combination of all characteristic/condition.
Can use the reactor drum of any kind that is suitable for hydrogen cracking to carry out said method.The instance of such reactor drum can include but not limited to trickle bed, liquid bed, moving-bed, fluidized-bed and slurry reactor.
Can from the product of hydrogen cracking, remove or reclaim one or more cuts as fuel composition of the present invention.In one embodiment, can be with the raw material hydrogen cracking with production and transport fuel.Said transport fuel also can be fractionated at least a fractionation component that for example is selected from gasoline, kerosene, rocket(engine)fuel, diesel oil and combination thereof.
In one embodiment, can carry out said method to produce or to reclaim the rocket(engine)fuel of kerosene type or gasoline types.In one embodiment, can carry out said method to produce or to reclaim ASTM D86 90% rectifying o'clock at 250 ℃ to 290 ℃, the preferred rocket(engine)fuel of the kerosene type in 260 ℃ to 280 ℃ scopes.Alternatively, can carry out said method to produce or to reclaim ASTM D86 90% rectifying o'clock at 200 ℃ to 240 ℃, the preferred rocket(engine)fuel of the gasoline types in 210 ℃ to 230 ℃ scopes.
In another embodiment, can carry out said method to produce or to reclaim ASTM D8610% rectifying o'clock at 150 ℃ to 200 ℃, the preferred rocket(engine)fuel of the kerosene type in 160 ℃ to 180 ℃ scopes.Alternatively, can carry out said method to produce or to reclaim ASTM D86 10% rectifying o'clock at 110 ℃ to 140 ℃, the preferred rocket(engine)fuel of the gasoline types in 120 ℃ to 130 ℃ scopes.
In another embodiment, can carry out said method to produce or to reclaim for example ASTMD8690% rectifying o'clock at 260 ℃ to 350 ℃, the preferred diesel oil fuel in 280 ℃ to 340 ℃ scopes.Alternatively, can carry out said method to produce or to reclaim ASTM D8610% rectifying o'clock at 200 ℃ to 240 ℃, the preferred diesel oil fuel in 210 ℃ to 230 ℃ scopes.
In addition or alternatively, the present invention includes following embodiment.
The method of 1. 1 kinds of production and transport fuel of embodiment, said method comprises: the raw material that contains lipid material and MO is provided, and wherein said lipid material is selected from tri-glyceride, fatty acid alkyl ester and combination thereof; And said raw material carried out hydrogen cracking with production and transport fuel.
The method of embodiment 2. embodiments 1, wherein said MO comprise straight run gas oil, vacuum gas oil, metallization removal oil, coker distillate, catalytic cracking distilled oil, heavy naphtha, diesel boiling range cut, rocket(engine)fuel boiling range cut, kerosene boiling range cut, coal slurry or its combination.
The method of embodiment 3. embodiments 1 or embodiment 2, wherein said raw material have at least 100 ℃ initial boiling point, are no more than 500 ℃ full boiling point or both.
Each method in embodiment 4. aforementioned embodiments, wherein based on the gross weight of said raw material, said raw material comprises the lipid material of at least 0.05 weight %.
Each method in embodiment 5. aforementioned embodiments, wherein based on the gross weight of said raw material, said raw material comprises the MO that is no more than 99 weight %.
Each method in embodiment 6. aforementioned embodiments, the lipid material of wherein said raw material partly comprises tri-glyceride, and based on the total tri-glyceride that exists in the said lipid material, the most of tri-glyceride that exists in the said lipid material is by C 8To C 22Fatty acid component constitutes.
Each method in embodiment 7. aforementioned embodiments, wherein based on the gross weight of lipid material in the said raw material, the lipid material of said raw material partly comprises the fatty acid alkyl ester of at least 20 weight %.
Each method in embodiment 8. aforementioned embodiments, wherein said transport fuel reclaims as at least a fractionation component that is selected from gasoline, kerosene, rocket(engine)fuel and diesel oil.
Each method in embodiment 9. aforementioned embodiments, it also comprises the step that said transport fuel is fractionated at least a fractionated fuel component that is selected from gasoline, kerosene, rocket(engine)fuel and diesel oil fuel.
Principle of the present invention and operation scheme are described in the above with reference to various exemplary and preferred implementations.As it is understood by one of ordinary skill in the art that whole invention, defined as claims, contained other preferred implementation of specifically not enumerating in this article.

Claims (9)

1. the method for a production and transport fuel, said method comprises: the raw material that contains lipid material and MO is provided, and wherein said lipid material is selected from tri-glyceride, fatty acid alkyl ester and combination thereof; And said raw material carried out hydrogen cracking with production and transport fuel.
2. the process of claim 1 wherein that said MO comprises straight run gas oil, vacuum gas oil, metallization removal oil, coker distillate, catalytic cracking distilled oil, heavy naphtha, diesel boiling range cut, rocket(engine)fuel boiling range cut, kerosene boiling range cut, coal slurry or its combination.
3. the method for claim 1 or claim 2, wherein said raw material have at least 100 ℃ initial boiling point, are no more than 500 ℃ full boiling point or both.
4. each method in the aforementioned claim, wherein based on the gross weight of said raw material, said raw material comprises the lipid material of at least 0.05 weight %.
5. each method in the aforementioned claim, wherein based on the gross weight of said raw material, said raw material comprises the MO that is no more than 99 weight %.
6. each method in the aforementioned claim, the lipid material of wherein said raw material partly comprises tri-glyceride, and based on the total tri-glyceride that exists in the said lipid material, the most of tri-glyceride that exists in the said lipid material is by C 8To C 22Fatty acid component constitutes.
7. each method in the aforementioned claim, wherein based on the gross weight of lipid material in the said raw material, the lipid material of said raw material partly comprises the fatty acid alkyl ester of at least 20 weight %.
8. each method in the aforementioned claim, wherein said transport fuel reclaims as at least a fractionation component that is selected from gasoline, kerosene, rocket(engine)fuel and diesel oil.
9. each method in the aforementioned claim, it also comprises the step that said transport fuel is fractionated at least a fractionated fuel component that is selected from gasoline, kerosene, rocket(engine)fuel and diesel oil fuel.
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