WO2010088486A1 - Valorisation sélective du brut-bio - Google Patents

Valorisation sélective du brut-bio Download PDF

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Publication number
WO2010088486A1
WO2010088486A1 PCT/US2010/022537 US2010022537W WO2010088486A1 WO 2010088486 A1 WO2010088486 A1 WO 2010088486A1 US 2010022537 W US2010022537 W US 2010022537W WO 2010088486 A1 WO2010088486 A1 WO 2010088486A1
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WO
WIPO (PCT)
Prior art keywords
oil
water
bio
hydrogen treatment
liquid product
Prior art date
Application number
PCT/US2010/022537
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English (en)
Inventor
Paul O'connor
Steve Yanik
Original Assignee
Kior Inc.
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Filing date
Publication date
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Publication of WO2010088486A1 publication Critical patent/WO2010088486A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen 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
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4087—Catalytic distillation
    • 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

Definitions

  • the invention relates generally to the upgrading of the liquid product obtained by pyrolysis of biomass material, and more particularly to the upgrading of the oily phase of the liquid pyrolysis product.
  • Biomass material in particular solid ligno-cellulosic biomass, is being studied as a feedstock for producing liquid fuel products.
  • pyrolysis the most promising route to preparing liquid products from ligno-cellulosic biomass is pyrolysis.
  • the pyrolysis reaction may be carried out with or without a catalyst. If carried out without a catalyst, the pyrolysis process is referred to as thermal pyrolysis. If carried out in the presence of a catalyst, the pyrolysis process is referred to as catalytic pyrolysis.
  • the pyrolysis reaction produces gaseous, liquid, and solid reaction products.
  • liquid fuels it is possible to convert biomass to a syngas, which in rum can be converted to a liquid fuel using a Fischer-Tropsch synthesis.
  • this route results in a high quality hydrocarbon fuel, the process is expensive.
  • US Patent 6,086,751 to Biensiock et al. discloses a process for treating TAN containing oils, e.g., crudes. By flashing to remove substantially all of the water therefrom, thermally treating the recovered liquid to reduce the naphthenic acid content thereof, and recombining light gases recovered from the flashing step with the treated liquid.
  • the '751 patent specifies that the thermal treatment is carried out in the absence of any catalyst for promoting the conversion of napfcthenic acids, in absence of any material added to react with or complex with uaphthenic acids, and in absence of absorbents for naphthenic acids.
  • the process disclosed in the '751 patent is unsuitable for upgrading liquid biomass pyrotysis products, because it is impossible to remove water therefrom by flashing, due to the hydrophilic nature of biomass pyrolysis products.
  • US Patent 6,063,266 to Grande et al. discloses a process for removing naphthenic acids from a crude oil.
  • the crude oil is hydrogenated at. 1 -SO bars and 100- 300 oC over a catalyst of the kind used for hydrogenation of atmospheric residue oils.
  • Preferred catalysts are Ni-Mo and Ni-Co, deposited on alumina as a earner material.
  • the catalyst used in the *26 ⁇ patent was not pre-sulfided. Although sulfur was present in the feedstock, the reaction was preferably carried out in such a way as to avoid the formation of H2S.
  • the TAN of the feedstock was reduced from 2.6 mg KOH/g to less than 0.5 mg KOH/g.
  • the pyrolysis oil was reacted with hydrogen at 300 oC for 15 minutes, and subsequently at 400 oC for 3 hours, Jn a representative nra with the Ni-Mo catalyst the oxygen content of the pyrolysis oil was reduced to 10.5 wt%.
  • the "oil” phase was subjected to a batch-wise hydrogenation reaction, using sulfide Co-Mo-P in gamma-alumina as catalyst
  • the upgraded oil was insoluble in methanol, soluble in toluene, and had an oxygen content of 3 wl%.
  • the quality of the liquid product can be improved further by forming an intimate mixture of the biomass material and a catalyst, prior to contacting the material with a hot catalyst for effecting the pyrolysis reaction.
  • This prior art process makes it possible to produce pyrolysis oil having a low enough Total Add Number to make it suitable for further processing in standard refinery processes and equipment
  • the operator may prefer to operate the process under conditions that produce a higher Total Acid Number, for example in order to further increase the liquid yield.
  • the present invention addresses these problems by providing a process for upgrading a liquid product of a biomass pyrolysis reaction, said liquid product comprising water and oxygenated hydrocarbons, said liquid product having an oxygen content of less than 30 wt%, said process comprising the steps of (i) allowing the liquid product to settle into an aqueous phase and an oi! phase; (ii) separating the oil phase from the aqueous phase; (iii) subjecting the oil phase to a hydrogen treatment step to form a mixture comprising low oxygen bio-oil and water; and (iv) removing water from the low oxygen bio ⁇ oil.
  • Another aspect of the invention is the low oxygen bio oil produced by the process of this invention.
  • Figure 1 shows a schematic diagram of a process for separating the oil phase and the aqueous phase of a bio-crude.
  • bio-crude contains significant amounts of water. Taking ligiio- ceUulosic biomass as an example, as harvested it contains generally from about 1 S to close to 50% water. Although it is possible to dry biomass material prior to using it as a feedstock in a pyrolysis reaction, drying is energy intensive and therefore costly. Even “dry” biomass still contains between 5 and 15% moisture. Drying the biomass further would require an inordinate amount of energy, and is therefore economically unattractive. Tn addition, very dry biomass presents a fire hazard, and handling difficulties due to the formation of static electricity, In general, therefore, biomass material used as a feedstock in pyrolysis reactions contains between 15 and 30% moisture, which is carried into the liquid product of the pyrolysis reaction.
  • a second difference between organics in crude and bio-crude is the high oxygen content of the organic components of bio-crude.
  • Cellulose has an oxygen content of about 44%, and the oxygen content of most forms of ligno-eeliulosic biomass is near 40%.
  • Standard pyrolysis processes produce a liquid product having high oxygen content, as reflected in a Total Acid Number in the range of from 50 to 70.
  • European Patent Application 08 153229.3-21.04 a liquid pyrolysis product can be produced having a Total Acid Number of less than 10. Although this product is of sufficient quality to be processed m standard refinery equipment, its oxygen content is still much higher than that of petroleum crude.
  • the present invention provides a process for upgrading bio-crude, said process comprising the steps of (i) allowing the liquid product to settle into an aqueous phase and an oil phase; (ii) separating the oil phase from the aqueous phase; (Hi) subjecting the oil phase to a hydrogen treatment step to form a mixture comprising low oxygen bio-oil and water, and (iv) removing the water from the low oxygen bio-oil.
  • the liquid product of a biomass pyrolysis reaction comprises water and oxygenated organic compounds. It is desirable to remove a significant portion of the water prior to subjecting the organic liquids to the hydrogen treatment step.
  • An important aspect of the present invention is the oxygen content of the liquid product, which is less than 30 wt%. This is considerably lower than the oxygen content of a typical flash pyrolysis oil, which is 40 wt% or more. As a result of this relatively low oxygen content the liquid product generally spontaneously separates into an aqueous phase and an oil phase, without requiring the inducement of phase separation. If water addition is needed to induce phase separation, the amount of water needed for inducement is far reduced, which facilitates the subsequent upgrading of the aqueous phase.
  • the water removal step generally requires just allowing the liquid product to settle into an aqueous phase and an oil phase.
  • Any phase separation technique may be used for this water removal step.
  • bio oil has a higher density than water.
  • Any technique for separating water from oil can be used for the present purpose, with the proviso that in the case of liquid pyrolysis products, the oil and water phases trade places because of the respective densities.
  • the density of a typical bio-oil is about 1.2.
  • FIG. 1 shows a skimming tank 10 that is suitable for use in the present invention.
  • Bio-crude 11 enters the skimming tank 10 at or near the top of the tank.
  • the tank is sized as a function of the flow rate of bio crude 11 to ensure a sufficient residence time in the tank. In general, the residence time should be at least about 10 minutes, and is preferably between about 30 minutes and about 60 minutes.
  • Tank inlet 18 at the top may be provided with a deflector (not shown) to minimize turbulence caused by the incoming liquid.
  • the oil phase 12 settles in the lower part of tank 10; the aqueous phase 13 collects at the top.
  • the two phases are separated by interface 14.
  • the oil phase leaves tank 10 via control valve 16,
  • the aqueous phase 13 leaves tank 10 via control valve 17.
  • the respective flow rates of oil phase 12 and aqueous phase 13 are controlled so that the level of interface 14 remains more or less constant.
  • the level of interface 14 may be allowed to vary during the operation of tank 10, provided that it does not rise to above the level of valve 17.
  • the oil phase recovered from step (ii) may still contain significant amounts of water.
  • the liquid product has a low oxygen content, its emulsifying properties are less, and the water removal steps (i) and (ii) result in the removal of a larger portion of the water.
  • De-emulsifiers are well known in the art. These materials generally act by reducing the surfactant properties of compounds having a hydrophilic portion and a lipophilic portion.
  • the surfactant properties of long chain carboxylic acids can be broken by the addition of a divalent metal ion, such as Ca or Mg.
  • a divalent metal ion such as Ca or Mg.
  • the water-solubility of divalent metal salts of long chain carboxylic acids is generally poor. Effectively, the addition of a divalent metal reduces the hydrophilic properties of the carboxylic acid.
  • the oil phase is subjected to a hydrogen treatment step.
  • This step comprises reacting the liquid with hydrogen.
  • mis reaction is carried out under a partial hydrogen pressure of at least about 34 bar.
  • the hydrogen treatment step is carried out in the presence of a catalyst.
  • suitable hydrogen treatment processes include hydrocracking and catalytic distillation.
  • Catalytic hydrocracking may be carried out in a fixed bed reactor.
  • the catalyst used in catalytic hydrocracking comprises a zeolite.
  • the hydrogen treatment reaction may also include the use of a hydrogenation catalyst.
  • the hydrogenation catalyst may be a conventional hydrotreatment catalyst.
  • the biomass feedstock may contain little or no nitrogen or sulfur compounds. Accordingly, there is little or no need for the hydrogen treatment to provide hydro- desulfurization activity and hydro- denitrogenation activity. Therefore, hydrogenation catalysts that have little or no desulfurization properties are suitable for use in the process of the present invention, although catalysts with desulfurization and/or denitrogenation activity would also be suitable tor use in the present invention.
  • Suitable examples include catalysts comprising platinum and other metals from the platinum group of the periodic table, such as Ru.
  • Nickel is another well known hydrogenation catalyst, and is preferred to platinum and similar metals because of its lower cost.
  • Preferred hydrogenation catalysts are those that contain nickel.
  • Reduced-metal hydrogenation catalysts tend to be susceptible to catalyst poisoning.
  • the more resilient traditional hydrotreatment catalysts are also suitable for use in the hydrogen treatment reaction of the process of the present invention.
  • Preferred examples include Co-Mo, Ni-Mo, and Ni-Co-Mo catalysts, for example on an alumina carrier.
  • the hydrotreatment catalyst preferably is introduced in its pre-sulfided form.
  • H2S hydrogen sulfide
  • DMS dimethyl sulfide
  • DMDS dimethyl disulfide
  • the sulfur compound can be selected from the group consisting of H2S, DMS, DMDS, and combinations thereof. Small amounts, in general in the range of from about 10 to about 50 ppm by weight of the feedstock, are sufficient to keep the catalyst sulfided.
  • Water is an important byproduct of the hydrogen treatment step, because most of the hydrogen is consumed by converting oxygen present in the organic compounds.
  • the oil phase from step ( ⁇ ) already contains significant amounts of water because of the incomplete removal during steps (i) and (n).
  • the emulsifying properties of the bio-oil are much reduced. Therefore, virtually all of the water now present in the bio oil can be removed by a skimming step as described herein above. If necessary, de ⁇ emulsifiers may be added to further improve the efficacy of this water removal step.
  • the low oxygen bio-oil produced by hydrogen treatment of the oil phase is suitable for blending in a diesel fuel, as oxygenated additives for gasoline, for heating oil, or for blending in kerosene, and the iike.
  • An important advantage of the process of the present invention is that the relatively expensive hydrogen treatment step is only used for the oil phase of the bio- crude.
  • the organic compounds in the oil phase have a lower oxygen content than the organic compounds dissolved in the aqueous phase.
  • the aqueous phase itself may be subjected to a de-oxygenation step.
  • the organic compounds present in the aqueous phase can be converted to noncorrosive oxygenated compounds that can be used in polymer chemistry and as oxygenated additives of gasoline.
  • the liquid pyrolysis product that is used as the feedstock for the present process is one having pH of about 4.S or higher. Feedstocks of this quality can be stored and processed in equipment made of stainless steel, or even soft steel, which represents a significant cost savings compared to the sophisticated alloys required for processing and storage of pyrolysis liquids having a lower pH.
  • Another advantage of using a feedstock having a pH of about 4,5 or higher is that the hydrogen consumed in the hydrogen treatment step is less, and that the hydrogen consumption results in an upgrading of the bio-oil in terms of heat content and hydrocarbon compatibility, rather than being required for stabilizing the bio-oil.

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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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention porte sur un procédé pour valoriser un produit liquide de pyrolyse de biomasse. Le procédé comprend la séparation du produit liquide en une phase aqueuse et une phase huileuse. La phase huileuse est soumise à une réaction de traitement par hydrogène, de préférence en présence d'un catalyseur. La bio-huile résultante est caractérisée par une faible teneur en oxygène.
PCT/US2010/022537 2009-01-29 2010-01-29 Valorisation sélective du brut-bio WO2010088486A1 (fr)

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US14808009P 2009-01-29 2009-01-29
US61/148,080 2009-01-29

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Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012166402A2 (fr) 2011-06-01 2012-12-06 Uop Llc Procédés et catalyseurs pour désoxygéner une huile de pyrolyse issue de biomasse
WO2012109034A3 (fr) * 2011-02-11 2012-12-06 Kior, Inc. Fioul renouvelable
WO2013049665A3 (fr) * 2011-09-30 2013-05-23 Chevron U.S.A., Inc. Procédé de production d'une bio-huile compatible avec un courant de raffinage à partir d'une charge d'alimentation lignocellulosique
US20140250774A1 (en) * 2013-03-08 2014-09-11 Upm-Kymmene Corporation Process for modifying bio-oil
WO2015023415A1 (fr) * 2013-08-16 2015-02-19 Kior, Inc. Procédé intégré de production de carburants de substitution renouvelables
WO2015038754A1 (fr) * 2013-09-11 2015-03-19 Research Triangle Institute Procédé et système de pyrolyse réactive catalytique rapide
EP2744873A4 (fr) * 2011-08-18 2015-12-23 Kior Inc Procédé de valorisation de produits dérivés de la biomasse
WO2016100395A1 (fr) * 2014-12-18 2016-06-23 Kior, Llc Procédé de thermolyse de biomasse en présence de sulfure d'hydrogène
US9382489B2 (en) 2010-10-29 2016-07-05 Inaeris Technologies, Llc Renewable heating fuel oil
US9387415B2 (en) 2011-08-18 2016-07-12 Inaeris Technologies, Llc Process for upgrading biomass derived products using liquid-liquid extraction
US9410216B2 (en) 2010-06-26 2016-08-09 Virdia, Inc. Sugar mixtures and methods for production and use thereof
US9447350B2 (en) 2010-10-29 2016-09-20 Inaeris Technologies, Llc Production of renewable bio-distillate
US9464238B2 (en) 2012-03-30 2016-10-11 Exxonmobil Research And Engineering Company Production of olefinic diesel, lubricants, and propylene
US9512495B2 (en) 2011-04-07 2016-12-06 Virdia, Inc. Lignocellulose conversion processes and products
US9598645B2 (en) 2012-03-30 2017-03-21 Exxonmobil Research And Engineering Company Coprocessing of biofeeds with group VI metal catalysts
US9617489B2 (en) 2011-02-11 2017-04-11 Inaeris Technologies, Llc Liquid bio-fuels
US9663836B2 (en) 2010-09-02 2017-05-30 Virdia, Inc. Methods and systems for processing sugar mixtures and resultant compositions
US9701594B2 (en) 2010-11-04 2017-07-11 Albemarle Europe Sprl Hydrodeoxygenation of pyrolysis oil in presence of admixed alcohol
US9708544B2 (en) 2012-03-30 2017-07-18 Exxonmobil Research And Engineering Company Production of olefinic diesel and corresponding oligomers
US10427069B2 (en) 2011-08-18 2019-10-01 Inaeris Technologies, Llc Process for upgrading biomass derived products using liquid-liquid extraction

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