EP2638127A1 - Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie - Google Patents

Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie

Info

Publication number
EP2638127A1
EP2638127A1 EP11779729.0A EP11779729A EP2638127A1 EP 2638127 A1 EP2638127 A1 EP 2638127A1 EP 11779729 A EP11779729 A EP 11779729A EP 2638127 A1 EP2638127 A1 EP 2638127A1
Authority
EP
European Patent Office
Prior art keywords
pyrolysis oil
equal
feed
hydrocarbon
pyrolysis
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.)
Withdrawn
Application number
EP11779729.0A
Other languages
English (en)
French (fr)
Inventor
Johannes Antonius Hogendoorn
Sascha Reinier Aldegonda Kersten
Ferran De Miguel Mercader
Colin John Schaverien
Nicolaas Wilhelmus Joseph Way
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 EP11779729.0A priority Critical patent/EP2638127A1/de
Publication of EP2638127A1 publication Critical patent/EP2638127A1/de
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • 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
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °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
    • C10G2300/1077—Vacuum residues
    • 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
    • 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
    • C10G2300/4006—Temperature
    • 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
    • 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 present invention relates to process for the preparation of a biofuel and/or biochemical.
  • the present invention provides processes to produce one or more cracked products from a pyrolysis oil.
  • renewable energy sources With the diminishing supply of crude mineral oil, use of renewable energy sources is becoming increasingly important for the production of fuels and chemicals. These fuels and chemicals from renewable energy sources are often referred to as biofuels, respectively biochemicals .
  • One of the advantages of using renewable energy sources is that the C02 balance is more favourable as compared with a conventional feedstock of a mineral source.
  • renewable energy sources such as lignocellulosic material, are preferred as these do not compete with food production.
  • biofuels and/or biochemicals are also referred to as second generation biofuels and/or biochemicals.
  • Lignocellulosic material such as wood
  • the present invention provides a process for the preparation of a biofuel and/or biochemical from a pyrolysis oil, which pyrolysis oil essentially has not been pretreated or upgraded by hydrotreatment and/or
  • Step i) can be carried out in various manners and
  • the current invention also provides several processes for producing the one or more cracked products.
  • the present invention provides a process to produce one or more cracked products comprising the steps of
  • hydrotreatment and/or hydrodeoxygenation or a part thereof containing in the range from equal to or more than 0 wt% to equal to or less than 25 wt% n-hexane
  • the present invention provides a process to produce one or more cracked products comprising the steps of
  • the processes of the invention advantageously allow for direct processing of pyrolysis oil, which essentially has not been pretreated or upgraded by hydrotreatment and/or hydrodeoxygenation, in a catalytic cracking unit, such as for example an FCC unit.
  • a catalytic cracking unit such as for example an FCC unit.
  • the process of the invention advantageously allows the pyrolysis oil to be processed in a catalytic cracking unit without the necessity of such a hydrotreatment and/or hydrodeoxygenation to substantially lower the oxygen content.
  • hydrocarbon co-feed can advantageously provide the hydrogen necessary to convert the oxygen in the pyrolysis oil into water.
  • the process is further advantageous in that going from the pyrolysis oil feed to the catalytic cracking products an extensive reduction in Total Acid Number (TAN) is
  • the processes according to the invention advantageously allow a simple, direct and economically interesting route towards the conversion of pyrolysis oil into biofuels and/or biochemicals .
  • step i) a pyrolysis oil is contacted with a catalytic cracking catalyst at a temperature of equal to or more than 400°C in the presence of a hydrocarbon co-feed to produce one or more cracked products.
  • a pyrolysis oil is herein understood an oil obtained by pyrolysis.
  • pyrolysis oil is preferably further understood an oil obtained by pyrolysis that has essentially not been pretreated or upgraded by hydrotreatment and/or hydrodeoxygenation .
  • hydrodeoxygenation to substantially reduce the oxygen content of the pyrolysis oil can advantageously be avoided in the processes according to the invention.
  • a pyrolysis oil is further understood a “whole" pyrolysis oil or a part thereof. As illustrated below, in certain embodiments it is preferred to use specific parts of a pyrolysis oil.
  • the pyrolysis oil is derived from a renewable energy source, that is, preferably the pyrolysis oil is obtained by pyrolysis of a renewable energy source.
  • the renewable energy source comprises a cellulosic material, more preferably a lignocellulosic material.
  • the pyrolysis oil is a pyrolysis oil derived from a
  • cellulosic material more preferably a lignocellulosic material .
  • Any suitable cellulose-containing material may be used as renewable energy source in the pyrolysis.
  • the cellulosic material may be obtained from a variety of plants and plant materials including agricultural wastes, forestry wastes, sugar processing residues and/or mixtures thereof. Examples of suitable cellulose-containing materials include
  • pyrolysis oil is obtained by
  • the wood and/or wood-related material contains bark and/or needles.
  • the pyrolysis oil is obtained by pyrolysis of wood and/or a wood-related material containing pine wood or forestry residue.
  • pyrolysis is herein understood the thermal decomposition of a, preferably renewable, energy source at a pyrolysis temperature of equal to or more than 350°C.
  • concentration of oxygen is preferably less than the concentration required for complete combustion. More preferably the pyrolysis is carried out in the essential absence of non-in-situ-generated oxygen. A limited amount of oxygen may be generated in-situ during the pyrolysis process.
  • pyrolysis is carried out in an atmosphere containing equal to or less than 5 vol.% oxygen, more preferably equal to or less than 1 vol.% oxygen and most preferably equal to or less than 0.1 vol.% oxygen. In a most preferred embodiment pyrolysis is carried out in the essential absence of oxygen.
  • the pyrolysis temperature is preferably equal to or more than
  • temperature is further preferably equal to or less 800°C, more preferably equal to or less than 700°C and most
  • the pyrolysis pressure may vary widely. For practical
  • the pyrolysis oil is provided by so-called fast or flash pyrolysis of the renewable energy source.
  • fast or flash pyrolysis preferably comprises rapidly heating the renewable energy source for a very short time and then rapidly reducing the temperature of the primary products before chemical equilibrium can occur.
  • pyrolysis products are obtained that may contain gas, solids (char) , one or more oily phase (s), and optionally an aqueous phase.
  • the oily phase (s) will hereafter be referred to as pyrolysis oil.
  • the pyrolysis oil can be separated from the pyrolysis products by any method known by the skilled person to be suitable for that purpose. This includes conventional methods such as filtration, centrifugation, cyclone separation, extraction, membrane separation and/or phase separation.
  • the pyrolysis oil may include for example carbohydrates, olefins, paraffins, oxygenates (such as aldehydes and/or carboxylic acids) and/or optionally some residual water.
  • the pyrolysis oil comprises carbon in an amount equal to or more than 25 wt%, more preferably equal to or more than 35wt%, and preferably equal to or less than 70 wt%, more preferably equal to or less than 60 wt% (on a dry basis ) .
  • the pyrolysis oil further preferably comprises hydrogen in an amount equal to or more than 1 wt%, more preferably equal to or more than 5wt%, and preferably equal to or less than 15 wt%, more preferably equal to or less than 10 wt% (on a dry basis ) .
  • the pyrolysis oil further preferably comprises oxygen in an amount equal to or more than 25 wt%, more preferably equal to or more than 35wt%, and preferably equal to or less than 70 wt%, more preferably equal to or less than 60 wt%.
  • oxygen content is preferably defined on a dry basis. By a dry basis is understood excluding water.
  • the pyrolysis oil may also contain nitrogen and/or sulphur. If nitrogen is present, the pyrolysis oil preferably
  • the pyrolysis oil preferably comprises sulphur in an amount equal to or more than 0.001 wt%, more preferably equal to or more than 0.01 wt%, and preferably equal to or less than 1 wt%, more preferably equal to or less than 0.1 wt% (on a dry basis) .
  • the pyrolysis oil preferably comprises water in an amount equal to or more than 0.1 wt%, more preferably equal to or more than lwt%, still more preferably equal to or more than 5 wt%, and preferably equal to or less than 55 wt%, more preferably equal to or less than 45 wt%, and still more preferably equal to or less than 35 wt%, still more
  • the pyrolysis oil of the present invention comprises aldehydes in an amount equal to or more than 5 wt%, more preferably equal to or more than 10wt%, and preferably equal to or less than 30 wt%, more preferably equal to or less than 20 wt%.
  • the pyrolysis oil comprises carboxylic acids in an amount equal to or more than 5 wt%, more preferably equal to or more than 10wt%, and preferably equal to or less than 25 wt%, more preferably equal to or less than 15 wt%.
  • the pyrolysis oil comprises carbohydrates in an amount equal to or more than 1 wt%, more preferably equal to or more than 5wt%, and preferably equal to or less than 20 wt%, more preferably equal to or less than 10 wt%.
  • the pyrolysis oil comprises phenols in an amount equal to or more than 0.1 wt%, more preferably equal to or more than 2wt%, and preferably equal to or less than 10 wt%, more preferably equal to or less than 5 wt%.
  • the pyrolysis oil comprises furfurals in an amount equal to or more than 0.1 wt%, more preferably equal to or more than lwt%, and preferably equal to or less than 10 wt%, more preferably equal to or less than 4 wt%.
  • hydrocarbon co-feed a co-feed that contains one or more hydrocarbon compounds (i.e.
  • hydrocarbon co-feed is preferably a liquid hydrocarbon co-feed.
  • a liquid hydrocarbon co-feed is understood a
  • hydrocarbon co-feed which is fed to a catalytic cracking unit essentially in the liquid phase.
  • the hydrocarbon co-feed can be any hydrocarbon feed known to the skilled person to be suitable as a feed for an
  • the hydrocarbon co-feed can for example be obtained from a conventional crude oil (also sometimes referred to as a petroleum oil or mineral oil), an unconventional crude oil (that is oil produced or extracted using techniques other than the traditional oil well method) or a renewable oil (that is oil derived from a renewable source) .
  • a conventional crude oil also sometimes referred to as a petroleum oil or mineral oil
  • an unconventional crude oil that is oil produced or extracted using techniques other than the traditional oil well method
  • a renewable oil that is oil derived from a renewable source
  • the hydrocarbon co-feed is derived from a, preferably conventional, crude oil.
  • the hydrocarbon co-feed is derived from a, preferably conventional, crude oil.
  • conventional crude oils include West Texas Intermediate crude oil, Brent crude oil, Caribbean-Oman crude oil, Midway Sunset crude oil or Tapis crude oil.
  • the hydrocarbon co-feed comprises a fraction of a, preferably conventional, crude oil or renewable oil.
  • fractions of a crude oil that can be used as a hydrocarbon co-feed include straight run (atmospheric) gas oils, flashed distillate, vacuum gas oils (VGO) , coker gas oils, atmospheric residue ("long residue”) and vacuum residue ("short residue”) and/or mixtures thereof.
  • VGO vacuum gas oils
  • hydrocarbon co-feed comprises comprises a long residue and/or a vacuum gas oil.
  • the hydrocarbon co-feed has an Initial Boiling Point (IBP) as measured by means distillation based on ASTM D2887-06a at a pressure of 1 bar absolute (0.1 MegaPascal) of equal to or more than 100°C,
  • IBP Initial Boiling Point
  • hydrocarbon co-feed is vacuum gas oil.
  • the hydrocarbon co-feed has an Initial Boiling Point (IBP) as measured by means of distillation based on ASTM D2887-06a at a pressure of 1 bar absolute (0.1 MegaPascal) equal to or more than 220°C, more preferably equal to or more than 240°C.
  • IBP Initial Boiling Point
  • An example of such a hydrocarbon co-feed is long residue.
  • composition of the hydrocarbon co-feed may vary
  • the hydrocarbon co-feed may for example contain paraffins, olefins and aromatics.
  • the hydrocarbon co-feed comprises equal to or more than 8 wt% elemental hydrogen, more
  • a high content of elemental hydrogen such as a content of equal to or more than 8 wt%, allows the hydrocarbon co-feed to act as a cheap hydrogen donor in the catalytic cracking process. Without wishing to be bound by any kind of theory it is further believed that a higher weight ratio of hydrocarbon co-feed to pyrolysis will enable more upgrading of the pyrolysis oil by hydrogen transfer reactions.
  • At least part of the hydrocarbon co- feed comprises a paraffinic hydrocarbon co-feed.
  • paraffinic hydrocarbon co-feeds include so-called Fischer-Tropsch derived hydrocarbon streams such as
  • the Fischer-Tropsch hydrocarbon stream may be any suitable Fischer-Tropsch hydrocarbon stream.
  • a fraction of a crude oil such as for example (atmospheric) gas oils, flashed distillate, vacuum gas oils (VGO) , coker gas oils, atmospheric residue ("long residue”) and vacuum residue ("short residue”)
  • a pyrolysis oil or a part thereof as described herein from equal to or more than 1 wt% to equal to or less than 35 wt%, preferably from equal to or more than 1 wt% to equal to or less than 20 wt% of a pyrolysis oil or a part thereof as described herein.
  • the weight ratio of the pyrolysis oil to hydrocarbon co- feed may vary widely.
  • the hydrocarbon co-feed and the pyrolysis oil are preferably being fed to a catalytic cracking unit in a weight ratio of hydrocarbon co-feed to pyrolysis oil of equal to or more than 50 to 50 (5:5), more preferably equal to or more than 70 to 30 (7:3), still more preferably equal to or more than 80 to 20 (8:2), even still more preferably equal to or more than 90 to 10 (9:1) .
  • the weight ratio of hydrocarbon co-feed to pyrolysis oil is preferably equal to or less than 99.9 to 0.1 (99.9:0.1) .
  • the amount of pyrolysis oil present is preferably equal to or less than 30 wt%, more preferably equal to or less than 20 wt%, most preferably equal to or less than 10 wt% and even more preferably equal to or less than 5 wt%.
  • amount of pyrolysis oil present is preferably equal to or more than 0.1 wt%.
  • step i) is carried out in a catalytic cracking unit, more preferably in a fluidized catalytic cracking (FCC) unit.
  • FCC fluidized catalytic cracking
  • the hydrocarbon co-feed and the pyrolysis oil can be mixed prior to entry into a catalytic cracking unit or they can be added separately, at the same location or different locations to the catalytic cracking unit.
  • pyrolysis oil are not mixed together prior to entry into a catalytic cracking unit.
  • the pyrolysis oil are not mixed together prior to entry into a catalytic cracking unit.
  • hydrocarbon co-feed and the pyrolysis oil may be fed simultaneously (that is at one location) to the catalytic cracking unit, and mixed upon entry of the catalytic cracking unit; or, alternatively, the hydrocarbon co-feed and the pyrolysis oil may be added separately (at
  • Catalytic cracking units can have multiple feed inlet nozzles.
  • the pyrolysis oil and the hydrocarbon co-feed can therefore be processed in the catalytic cracking unit even if both components are not miscible by feeding each component through a separate feed inlet nozzle.
  • the pyrolysis oil can be mixed with a, preferably liquid, hydrocarbon co-feed.
  • the pyrolysis oil preferably comprises less than 25wt% n-hexane extractives; comprises a bottom phase of a pyrolysis oil; and/or is a pyrolysis oil which when combined with a, preferably liquid, hydrocarbon co-feed provides a combination that has a molar ratio of hydrogen to carbon of at least 1 to 1.
  • the pyrolysis oil preferably comprises less than 25wt% n-hexane extractives; comprises a bottom phase of a pyrolysis oil; and/or is a pyrolysis oil which when combined with a, preferably liquid, hydrocarbon co-feed provides a combination that has a molar ratio of hydrogen to carbon of at least 1 to 1.
  • hydrocarbon co-feed and the pyrolysis oil are mixed together prior to entry into a catalytic cracking unit to provide a feed mixture comprising the hydrocarbon co-feed and the pyrolysis oil.
  • the hydrocarbon co-feed and the pyrolysis oil are preferably mixed at a temperature in the range between equal to or more than 10°C, more preferably equal to or more than 20°C, still more preferably equal to or more than 30°C and most preferably preferably equal to or more than 40°C, and equal to or less than 80 °C, more preferably equal to or less than 70°C and most preferably equal to or less than 60°C.
  • a temperature in the range from 10°C to 25°C is preferred, whereas when the feed mixture contains Long Residue a temperature in the range from 30°C to 50°C is preferred.
  • the hydrocarbon co-feed and the pyrolysis oil may be mixed in any manner known to be skilled person to be suitable for such purpose.
  • the hydrocarbon co-feed and the pyrolysis oil are mixed by means of static mixing, shaking and/or stirring.
  • the feed mixture may optionally be held in a stirred or non-stirred feed vessel before being forwarded to a catalytic cracking unit. It is one of the advantages of the process according to the present invention that also a non-stirred feed vessel may be used, thereby obtaining a more simple operation process and/or saving upon
  • the feed mixture is held in such a stirred or non-stirred feed vessel at a temperature in the range between equal to or more than 10°C, more preferably equal to or more than 20°C, still more preferably equal to or more than 30°C and most preferably preferably equal to or more than 40°C, and equal to or less than 80 °C, more preferably equal to or less than 70°C and most preferably equal to or less than 60°C.
  • the feed mixture contains VGO as a hydrocarbon co-feed
  • a slightly lower temperature of equal to or more than 10°C may be preferred, whereas when the feed mixture contains Long Residue a slightly higher temperature of equal to or more than 30° may be preferred.
  • a temperature in the range from 10°C to 25°C is preferred, whereas when the feed mixture contains Long Residue a temperature in the range from 30°C to 50°C is preferred.
  • the feed mixture is injected into the catalytic cracking unit, optionally after being held in a stirred or non-stirred feed vessel, at a temperature in the range between equal to or more than 10°C, more preferably equal to or more than 20°C, still more preferably equal to or more than 30°C and most preferably preferably equal to or more than 40°C, and equal to or less than 80 °C, more preferably equal to or less than 70°C and most preferably equal to or less than 60°C.
  • VGO as a hydrocarbon co-feed
  • a slightly lower temperature of equal to or more than 10°C may be preferred, whereas when the feed mixture contains Long Residue a slightly higher temperature of equal to or more than 30° may be preferred.
  • a temperature in the range from 10°C to 25°C is preferred, whereas when the feed mixture contains Long Residue a temperature in the range from 30°C to 50°C is preferred.
  • the feed mixture may be contacted with the catalytic cracking catalyst in a catalytic cracking unit.
  • the catalytic cracking catalyst can be any catalyst known to the skilled person to be suitable for use in a cracking process.
  • the catalytic cracking catalyst comprises a zeolitic component.
  • the catalytic cracking catalyst can contain an amorphous binder compound and/or a filler. Examples of the amorphous binder
  • component include silica, alumina, titania, zirconia and magnesium oxide, or combinations of two or more of them.
  • fillers include clays (such as kaolin) .
  • the zeolite is preferably a large pore zeolite.
  • the large pore zeolite includes a zeolite comprising a porous, crystalline aluminosilicate structure having a porous internal cell structure on which the major axis of the pores is in the range of 0.62 nanometer to 0.8 nanometer.
  • the axes of zeolites are depicted in the x Atlas of Zeolite Structure Types', of W.M. Meier, D.H. Olson, and Ch.
  • USY is preferably used as the large pore zeolite.
  • the catalytic cracking catalyst can also comprise a medium pore zeolite.
  • the medium pore zeolite that can be used according to the present invention is a zeolite comprising a porous, crystalline aluminosilicate structure having a porous internal cell structure on which the major axis of the pores is in the range of 0.45 nanometer to 0.62 nanometer.
  • Examples of such medium pore zeolites are of the MFI structural type, for example, ZSM-5; the MTW type, for example, ZSM-12; the TON structural type, for example, theta one; and the FER structural type, for example, ferrierite.
  • ZSM-5 is preferably used as the medium pore zeolite.
  • a blend of large pore and medium pore zeolites may be used.
  • the ratio of the large pore zeolite to the medium pore size zeolite in the cracking catalyst is preferably in the range of 99:1 to 70:30, more preferably in the range of 98:2 to 85:15.
  • the total amount of the large pore size zeolite and/or medium pore zeolite that is present in the cracking catalyst is preferably in the range of 5 wt% to 40 wt%, more preferably in the range of 10 wt% to 30 wt%, and even more preferably in the range of 10 wt% to 25 wt% relative to the total mass of the catalytic cracking catalyst.
  • the pyrolysis oil is preferably contacted with the
  • reaction zone which reaction zone is preferably an elongated tube-like reactor, preferably oriented in an essentially vertical manner.
  • the pyrolysis oil, the hydrocarbon co-feed and the cracking catalyst may each independently flow in an upward
  • the pyrolysis oil and the hydrocarbon co-feed flow co-currently in the same direction.
  • the catalytic cracking catalyst can be contacted in a
  • the catalytic cracking catalyst is contacted in a cocurrent flow configuration with a cocurrent flow of the pyrolysis oil and the liquid hydrocarbon cofeed.
  • step i) comprises:
  • a catalytic cracking step wherein the pyrolysis oil and the hydrocarbon co-feed are cracked in a reaction zone in the presence of the catalytic cracking catalyst to produce one or more cracked products and a spent catalytic
  • the temperature in the catalytic cracking step preferably ranges from equal to or more than 450 °C to equal to or less than 650 °C, more preferably from equal to or more than 480 °C to equal to or less than 600 °C, and most preferably from equal to or more than 480 °C to equal to or less than 560 °C.
  • the pressure in the catalytic cracking step preferably ranges from equal to or more than 0.5 bar to equal to or less than 10 bar (0.05 MPa-1 MPa) , more preferably from equal to or more than 1.0 bar to equal to or less than 6 bar (0.15 MPa to 0.6 MPa) .
  • the residence time of the catalytic cracking catalyst in the reaction zone, where the catalytic cracking takes place preferably ranges from equal to or more than 0.1 seconds to equal to or less than 15 seconds, more
  • the mass ratio of the catalytic cracking catalyst to the total feed of pyrolysis oil Preferably, the mass ratio of the catalytic cracking catalyst to the total feed of pyrolysis oil and
  • hydrocarbon co-feed ranges from equal to or more than 3 to equal to or less than 20.
  • the mass ratio of the catalytic cracking catalyst to the total feed of pyrolysis oil and hydrocarbon co-feed is at least 3.5. The use of a higher catalyst to feed mass ratio results in an increase in conversion.
  • the catalytic cracking step further comprises a stripping step.
  • the spent catalyst may be stripped to recover the products absorbed on the spent catalyst before the regeneration step. These products may be recycled and added to the product stream obtained from the catalytic cracking step.
  • the regeneration step preferably comprises burning off of coke, deposited on the catalyst as a result of the
  • the heat generated in the exothermic regeneration step is preferably employed to provide energy for the endothermic catalytic cracking step.
  • the process according to the invention advantageously allows for a sufficient amount of coke deposited on the catalytic cracking catalyst such that the exothermic regeneration step can be carried out without supplying additional heat.
  • the regeneration temperature preferably ranges from equal to or more than 575 °C to equal to or less than 900 °C, more preferably from equal to or more than 600 °C to equal to or less than 850 °C.
  • the pressure in the regenerator preferably ranges from equal to or more than 0.5 bar to equal to or less than 10 bar (0.05 MPa to 1 MPa) , more preferably from equal to or more than 1.0 bar to equal to or less than 6 bar (0.1 MPa to 0.6 MPa) .
  • the regenerated catalytic cracking catalyst can be any suitable material.
  • the regenerated catalytic cracking catalyst can be any suitable material.
  • a side stream of make-up catalyst is added to such a recycle stream of regenerated catalytic cracking catalyst to make-up for loss of catalyst in the reaction zone and regenerator.
  • step i) can be carried out in various manners .
  • the part of or whole pyrolysis oil in step i) comprises a pyrolysis oil or a part thereof containing equal to or less than 25 wt% n-hexane
  • step i) therefore comprises a process to produce one or more cracked products comprising the steps of
  • n-hexane extractives are herein understood compounds extractable from the pyrolysis oil into n-hexane (normal- hexane) at a temperature of about 20°C and a pressure of about 1 bar absolute (0.1 MegaPascal) .
  • n-Hexane normal- hexane
  • extractives can be determined according to Oasmaa et al, in their article titled “Fast Pyrolysis of Forestry
  • n-hexane extractives examples include rubbers, tannins, flavonoids, lignin monomers (such as guaiacol and catechol derivatives), lignin dimers (stilbenes), resin, waxes, sterols, vitamins and fungi.
  • lignin monomers such as guaiacol and catechol derivatives
  • lignin dimers stilbenes
  • resin waxes, sterols, vitamins and fungi.
  • the pyrolysis oil or a part thereof contains in the range from equal to or more than 0 wt% to equal to or less than 25 wt% n-hexane extractives, more preferably in the range from equal to or more than 0 wt% to equal to or less than 20 wt% n-hexane extractives, still more
  • n-hexane extractives preferably in the range from equal to or more than 0 wt% to equal to or less than 15 wt% n-hexane extractives, still more preferably in the range from equal to or more than 0 wt% to equal to or less than 10 wt% n-hexane extractives, even still more preferably in the range from equal to or more than 0 wt% to equal to or less than 6 wt% n-hexane extractives, and most preferably in the range from equal to or more than 0 wt% to equal to or less than 3 wt% n-hexane extractives.
  • a lower limit of equal to or more than 0.01 ppm by weight may be considered more preferably in the above ranges, and a lower limit of equal to or more than 0.1 ppm by weight may be considered most preferably in the above ranges.
  • the pyrolysis oil or part thereof contains essentially no n-hexane extractives .
  • the pyrolysis oil or part thereof, containing equal to or less than 25 wt% n-hexane extractives, can be obtained in any manner known by the skilled person to be suitable for this purpose.
  • extractives may be obtained by solvent extraction of the n-hexane extractives from a pyrolysis oil or part thereof, containing more than 25 wt% n-hexane extractives.
  • Solvents suitable in such solvent extraction include n-hexane but also other hexanes, heptanes, pentanes, octanes, nonanes or decanes.
  • solvents such as acetone and or dichloromethane may be helpful.
  • the pyrolysis oil or part thereof may be phase separated as described in more detail below, to produce a bottom phase pyrolysis oil containing in the range from equal to or more than 0 wt% to equal to or less than 25 wt% n-hexane extractives, preferably in the range from equal to or more than 0 wt% to equal to or less than 20 wt% n-hexane extractives, more preferably in the range from equal to or more than 0 wt% to equal to or less than 15 wt% n-hexane extractives, still more preferably in the range from equal to or more than 0 wt% to equal to or less than 10 wt% n-hexane extractives and most preferably in the range from equal to or more than 0 wt% to equal to or less than 6 wt% n-hexane extractives; and a top phase pyrolysis oil preferably containing more than 25 wt% n- hexane
  • Residue 1 Effect of extractives on phase separation of pyrolysis liquids", first published in Energy & Fuels, an American Chemical Society journal, volume 17, number 1 January-February 2003, pages 1-12.
  • the part of or whole pyrolysis oil in step i) comprises only a bottom phase pyrolysis oil or a part thereof.
  • step i) therefore comprises a process to produce one or more cracked products comprising the steps of
  • step 2a a bottom phase of a pyrolysis oil is provided.
  • the bottom phase of a pyrolysis oil is understood the lowest of the phases that can be obtained when phase
  • phase separation may take place because of significant polarity, solubility and
  • the bottom phase of a pyrolysis oil is sometimes also referred to as bottom phase pyrolysis oil.
  • the bottom phase pyrolysis oil can be obtained from a pyrolysis oil that is suitable for phase separation into at least a top phase and a bottom phase.
  • a pyrolysis oil that is suitable for phase separation into at least a top phase and a bottom phase is also understood a pyrolysis oil that can be separated into at least a top phase and a bottom phase with the help of a separation agent.
  • the pyrolysis oil is a pyrolysis oil that can be separated into at least a top phase and a bottom phase without requiring the pyrolysis oil to be contacted with a separation agent.
  • the pyrolysis oil is phase separated into at least a top phase and a bottom phase to produce a top
  • phase pyrolysis oil and a bottom phase pyrolysis oil.
  • the invention provides a process to produce one or more cracked products comprising the steps of
  • pyrolysis oil or part thereof has essentially not been pretreated or upgraded by hydrotreatment and/or
  • phase separation can be brought about by contacting the pyrolysis oil with a separation agent.
  • a separation agent is understood a compound that assists in the separation of the pyrolysis oil into one or more phases.
  • such separation agent is an alcohol.
  • alcohols that can be used as a separation agent include ethanol and isopropanol.
  • isopropanol can be used as a separation agent is provided by Oasmaa et al in their article titled "Fast Pyrolysis of Forestry Residue and Pine. 4.
  • an alcohol is preferably present in an amount of equal to or more than 0.25 wt%, more preferably equal to or more than 0.5 wt%, still more preferably equal to or more than 1 wt% and most preferably equal to or more than 2 wt%, based on the total combination of alcohol and pyrolysis oil; and preferably in an amount of equal to or less than 10 wt%, more preferably equal to or less than 7 wt% and most preferably equal to or less than 5 wt%, based on the total combination of alcohol and pyrolysis oil.
  • phase separation can be brought about by lowering the temperature (cooling) of the
  • the pyrolysis oil after production. If phase separation is brought about by cooling, the pyrolysis oil is preferably cooled to a temperature equal to or above 15 °C, more preferably equal to or above 25°C and preferably equal to or below 50°C, more preferably equal to or below 45°C.
  • An example of how cooling can be used to separate phases is provided by Oasmaa et al in their article titled " Fast Pyrolysis of Forestry Residue. 1. Effect of Extractives on Phase Separation of Pyrolysis Liquids", Energy and Fuels 2003, volume 17, pages 1 to 12.
  • the bottom phase pyrolysis oil can subsequently be
  • phase separation methods include settling, decantation, centrifugation, cyclone separation, extraction and membrane techniques.
  • the bottom phase pyrolysis oil which is being contacted with the catalytic cracking catalyst at a temperature of equal to or more than 400°C in the presence of a hydrocarbon co- feed to produce one or more cracked products, may be contaminated with minor amounts of other phases than the bottom phase pyrolysis oil.
  • These minor amounts of the other phases may for example be dispersed or dissolved in the bottom phase pyrolysis oil.
  • invention consists for equal to or more than 90 wt%, more preferably for equal to or more than 95 wt%, even more preferably equal to or more than 99 wt%, still more preferably equal to or more than 99.9 wt% and most
  • bottom phase pyrolysis oil preferably equal to or more than 99.99 wt% of bottom phase pyrolysis oil, based on the total weight of pyrolysis oil being contacted with the catalytic cracking catalyst.
  • the amount of any other phase pyrolysis oils is equal to or less than 10 wt%, more preferably equal to or less than 5 wt%, even more preferably equal to or less than 1 wt%, still more preferably equal to or less than 0.1 wt% and most preferably equal to or less than 0.01 wt%, based on the total weight of pyrolysis oil being contacted with the catalytic cracking catalyst.
  • any pyrolysis oil being contacted with the catalytic cracking catalyst in the process of the invention consists essentially only of bottom phase pyrolysis oil. That is, most preferably the catalytic cracking is carried out in the essential absence of any non-bottom phase pyrolysis oil.
  • An example of a non-bottom phase pyrolysis oil is the top phase pyrolysis oil.
  • the bottom phase pyrolysis oil contains in the range from equal to or more than 0 wt% to equal to or less than 25 wt% n-hexane extractives, more preferably in the range from equal to or more than 0 wt% to equal to or less than 20 wt% n-hexane extractives, still more preferably in the range from equal to or more than 0 wt% to equal to or less than 15 wt% n-hexane extractives, still more preferably in the range from equal to or more than 0 wt% to equal to or less than 10 wt% n- hexane extractives, even still more preferably in the range from equal to or more than 0 wt% to equal to or less than 6 wt% n-hexane extractives, and most preferably in the range from equal to or more than 0 wt% to equal to or less than 3 wt% n-hexane extractives.
  • bottom phase pyrolysis oil may contain water (preferably in the range from 20-35 wt%), carboxylic acids (preferably in the range from 5-15 wt%), alcohols
  • carbohydrates preferably in the range from (25-40 wt%), and/or lignin compounds (preferably in the range from 5-30wt%) .
  • step i) is a pyrolysis oil or part thereof which when combined with a, preferably liquid, hydrocarbon co-feed provides a combination that has a molar ratio of hydrogen to carbon of at least 1 to 1.
  • step i) therefore comprises a process to produce one or more cracked products comprising the steps of
  • the combination of the pyrolysis oil or part thereof and the, preferably liquid, hydrocarbon co-feed preferably has an overall molar ratio of hydrogen to carbon (H/C) of equal to or more than 1.1 to 1 (1.1/1), more preferably of equal to or more than 1.2 to 1 (1.2/1), most preferably of equal to or more than 1.3 to 1 (1.3/1) .
  • H/C overall molar ratio of hydrogen to carbon
  • an effective molair ratio of hydrogen to carbon (H/C eff ) is used.
  • H/C eff the effective molair ratio of hydrogen to carbon
  • the combination of the pyrolysis oil or part thereof and the, preferably liquid, hydrocarbon co-feed has an overall effective molair ratio of hydrogen to carbon (H/C eff ) of equal to or more than 1 to 1, more preferably of equal to or more than 1.1 to 1 (1.1/1), even more preferably of equal to or more than 1.2 to 1 (1.2/1), most preferably of equal to or more than 1.3 to 1 (1.3/1) .
  • the desired molar ratio of hydrogen to carbon (H/C) or desired effective molar ratio of hydrogen to carbon (H/C eff ) can be obtained by using a specific hydrocarbon co-feed. Examples of suitable hydrocarbon co- feeds are listed above. A most preferred hydrocarbon co- feed in this respect is a Long Residue.
  • the desired molar ratio of hydrogen to carbon (H/C) or desired effective molar ratio of hydrogen to carbon (H/C eff ) can be obtained by using a specific weight ratio of the pyrolysis oil to the
  • hydrocarbon co-feed examples of suitable weight ratios of the pyrolysis oil to the hydrocarbon co-feed are listed above. Most preferred weight ratios of the hydrocarbon co- feed to the pyrolysis oil in this respect lie in the range from 7:3 to 9:1.
  • step i) of the process according to the invention one or more cracked products are produced.
  • These one or more cracked products can be further processed in any manner known to the skilled person to be suitable for further processing these products.
  • Such further processing may for example include fractionating and/or hydrotreating (such as for example hydrodesulphurization, hydrode- nitrogenation, hydrodeoxygenation and/or
  • the one or more cracked products are any one or more cracked products.
  • product fractions include drygas (including carbon monoxide, carbon dioxide, methane, ethane, ethene, hydrogen sulfide and hydrogen), LPG (including propane and butanes with small amounts of propene and butenes),), gasoline (boiling in the range from C5 to 221°C), light cycle oils (LCO; boiling in the range from 221°C to
  • the one or more cracked products contain in the range from equal to or more than 20 wt% to equal to or less than 90 wt% of gasoline and LCO, more preferably in the range from equal to or more than 30 wt% to equal to or less than 80 wt% of gasoline and LCO.
  • the product fractions, obtained after fractionating the one or more cracked products can be used to produce a biofuel and/or a biochemical.
  • one or more product fractions can be blended with one or more other components to produce a biofuel and/or a biochemical .
  • a fuel respectively a chemical that is at least partly derived from a renewable energy source.
  • Examples of one or more other components with which the one or more product fractions may be blended include anti ⁇ oxidants, corrosion inhibitors, ashless detergents, dehazers, dyes, lubricity improvers and/or mineral fuel components .
  • the present invention further comprises combinations of the embodiments described in the description above.
  • the invention is illustrated by the following non-limiting examples .
  • Example 1 Mixing bottom phase pyrolysis oil derived from forest residue and a hydrocarbon feed.
  • a pyrolysis oil derived from forest residue was obtained from VTT. Pyrolysis of the forest residue was carried out using a
  • VGO vacuum gas oil
  • the glass bottle was turned upside down to see if there were two separate layers of liquid visible.
  • a dark brown sticky material on the bottom of the glass bottle indicates non-miscibility of the pyrolysis oil fraction.
  • Table 4 shows the visual test results of the miscibility of 20% top phase pyrolysis oil from forest residue with VGO and of 20% bottom phase pyrolysis oil from forest residue with Heavy feed mixture.
  • Example 2 Catalytic cracking of a mixture of top phase pyrolysis oil from forest residue with VGO in a non-stirred feed vessel.
  • the mixture of 20 wt% top phase pyrolysis oil from forest residue with 80 wt% vacuum gas oil (VGO) as prepared under example 1 was transferred as a feed mixture to the feed vessel of a MAT-5000 fluidized catalytic cracking unit.
  • the feed vessel was kept at 60 °C during transfer. The feed vessel was not stirred.
  • a first test run was started
  • the first test run included the 7 experiments with 7 catalyst to oil ratios, namely catalyst/oil ratios of 3, 4, 5, 6, 6.5, 7 and 8.
  • the fluidized catalyst bed was kept at 500 °C .
  • the liquid FCC products were collected in glass receivers at minus 18-19 °C.
  • the FCC catalyst was stripped with nitrogen during 11 minutes.
  • the gas produced during such stripping was weighted and analyzed online with a gas chromatograph (GC) .
  • GC gas chromatograph
  • the FCC catalyst was regenerated in-situ at 650 °C for 40 minutes in the presence of air.
  • the LPG, gasoline and coke make in the 1st and 2nd run show substantial differences.
  • the poor reproducibility for the 1st and 2nd test run in example 2 indicates a poor miscibility of the top phase pyrolysis oil and the VGO.
  • the process in example 5 may therefore be less robust when upscaling to a commercial scale.
  • Example 3 Catalytic cracking of a mixture of bottom phase pyrolysis oil from forest residue with Heavy feed mixture in a non-stirred feed vessel.
  • the mixture of 20 wt% bottom phase pyrolysis oil from forest residue with 80 wt% Heavy feed mixture as prepared under example 1 was transferred as a feed mixture to the feed vessel of a MAT-5000 fluidized catalytic cracking unit.
  • a process identical to that described for example 2 was carried out except that for example 3 the fluidized catalyst bed during catalytic cracking was kept at 520 °C instead of 500
  • the process according to the invention may also advantageously enable further downstream processing of the catalytically cracked pyrolysis oil in a refinery .
  • Example 4 Mixing bottom phase pyrolysis oil derived from pine and a liquid hydrocarbon feed.
  • a pyrolysis oil derived from pine was obtained from VTT.
  • Example 5 Catalytic cracking of a mixture of bottom phase pyrolysis oil derived from pine and Heavy feed mixture in a non-stirred and in a stirred feed vessel.
  • Example 6 Catalytic cracking of a mixture of bottom phase pyrolysis oil and Heavy feed mixture on a pilot scale.
  • the above feed was heated to 82°C and transferred as a feed mixture to the feed vessel of a pilot-scale fluidized catalytic cracking unit.
  • the pilot- scale fluidized catalytic cracking unit consisted of six sections including a feed supply system, a catalyst loading and transfer system, a riser reactor, a stripper, a product separation and collecting system, and a regenerator.
  • the riser reactor was an adiabatic riser having an inner diameter of 11 mm and a length of about 3.2 m.
  • the riser reactor outlet was in fluid communication with the stripper that was operated at the same temperature as the riser reactor outlet flow and in a manner so as to provide essentially 100 percent stripping efficiency.
  • the regenerator was a multi-stage continuous regenerator used for regenerating the spent catalyst.
  • the spent catalyst was fed to the regenerator at a controlled rate and the regenerated catalyst was collected in a vessel.
  • the catalytic cracking catalyst cntained ultra stable zeolite Y.
  • est 100 °C, est determine

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP11779729.0A 2010-11-12 2011-11-11 Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie Withdrawn EP2638127A1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP11779729.0A EP2638127A1 (de) 2010-11-12 2011-11-11 Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP10191114 2010-11-12
PCT/EP2011/069985 WO2012062924A1 (en) 2010-11-12 2011-11-11 Process for the preparation of a biofuel and/or biochemical
EP11779729.0A EP2638127A1 (de) 2010-11-12 2011-11-11 Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie

Publications (1)

Publication Number Publication Date
EP2638127A1 true EP2638127A1 (de) 2013-09-18

Family

ID=43993164

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11779729.0A Withdrawn EP2638127A1 (de) 2010-11-12 2011-11-11 Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie

Country Status (6)

Country Link
EP (1) EP2638127A1 (de)
JP (1) JP2013545841A (de)
CN (1) CN103201357A (de)
BR (1) BR112013011287A2 (de)
CA (1) CA2816353A1 (de)
WO (1) WO2012062924A1 (de)

Families Citing this family (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3252128B1 (de) 2006-04-03 2019-01-02 Pharmatherm Chemicals Inc. Thermales extrationsverfahren zur herstellung eines taxanextrakts
US20110284359A1 (en) 2010-05-20 2011-11-24 Uop Llc Processes for controlling afterburn in a reheater and for controlling loss of entrained solid particles in combustion product flue gas
US8499702B2 (en) 2010-07-15 2013-08-06 Ensyn Renewables, Inc. Char-handling processes in a pyrolysis system
WO2012092468A1 (en) * 2010-12-30 2012-07-05 Kior Inc. Production of renewable biofuels
US9441887B2 (en) 2011-02-22 2016-09-13 Ensyn Renewables, Inc. Heat removal and recovery in biomass pyrolysis
US9347005B2 (en) 2011-09-13 2016-05-24 Ensyn Renewables, Inc. Methods and apparatuses for rapid thermal processing of carbonaceous material
US9109177B2 (en) 2011-12-12 2015-08-18 Ensyn Renewables, Inc. Systems and methods for renewable fuel
US9670413B2 (en) 2012-06-28 2017-06-06 Ensyn Renewables, Inc. Methods and apparatuses for thermally converting biomass
US10166519B2 (en) * 2012-07-31 2019-01-01 Uop Llc Methods and fuel processing apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream
US9663729B2 (en) 2012-07-31 2017-05-30 Uop Llc Methods and fuel processing apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream
WO2014064109A1 (en) * 2012-10-25 2014-05-01 Shell Internationale Research Maatschappij B.V. Feed nozzle assembly for a catalytic cracking reactor
CN103773496B (zh) * 2012-10-25 2017-03-22 中国石油大学(北京) 用于催化裂化热解油的方法
FI125589B2 (en) * 2013-04-08 2022-03-31 Stora Enso Oyj Processes for deoxidation of bio-based materials and production of bio-based terephthalic acid and olefinic monomers
WO2014210150A1 (en) 2013-06-26 2014-12-31 Ensyn Renewables, Inc. Systems and methods for renewable fuel
CN103409163B (zh) * 2013-07-29 2015-11-18 江苏大学 一种生物原油的精制方法
CN103394505B (zh) * 2013-08-05 2015-04-29 中国科学院城市环境研究所 一种利用植物控制修复土壤并产生生物燃料的方法
KR102385590B1 (ko) 2014-07-17 2022-04-11 사빅 글로벌 테크놀러지스 비.브이. 수소열분해 공정에서 수소 도너 스트림을 사용한 수소 결핍 스트림의 업그레이드
US10337726B2 (en) 2015-08-21 2019-07-02 Ensyn Renewables, Inc. Liquid biomass heating system
MY193949A (en) 2016-12-29 2022-11-02 Ensyn Renewables Inc Demetallization Of Liquid Biomass
US11401474B2 (en) 2017-04-13 2022-08-02 Alliance For Sustainable Energy, Llc Systems and methods for producing fuel intermediates
EP3421572B1 (de) * 2017-06-29 2020-08-12 Neste Oyj Verfahren zur erhöhung der benzin- und mitteldestillatselektivität beim katalytischen cracken
US10696906B2 (en) 2017-09-29 2020-06-30 Marathon Petroleum Company Lp Tower bottoms coke catching device
FI127783B (en) 2017-11-27 2019-02-28 Neste Oyj Manufacture of a mixture of fuels
US12000720B2 (en) 2018-09-10 2024-06-04 Marathon Petroleum Company Lp Product inventory monitoring
US12031676B2 (en) 2019-03-25 2024-07-09 Marathon Petroleum Company Lp Insulation securement system and associated methods
US11975316B2 (en) 2019-05-09 2024-05-07 Marathon Petroleum Company Lp Methods and reforming systems for re-dispersing platinum on reforming catalyst
WO2021092309A1 (en) * 2019-11-07 2021-05-14 Eastman Chemical Company Recycle content propanol
US11124714B2 (en) 2020-02-19 2021-09-21 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
GB2602485B (en) * 2020-12-31 2023-06-14 Abundia Biomass To Liquids Ltd Converting biomass to gasoline
US11702600B2 (en) 2021-02-25 2023-07-18 Marathon Petroleum Company Lp Assemblies and methods for enhancing fluid catalytic cracking (FCC) processes during the FCC process using spectroscopic analyzers
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US20220268694A1 (en) 2021-02-25 2022-08-25 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US12018216B2 (en) 2021-10-10 2024-06-25 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using plastic
US12037548B2 (en) 2021-10-10 2024-07-16 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11692141B2 (en) 2021-10-10 2023-07-04 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
FR3145360A1 (fr) 2023-01-27 2024-08-02 Totalenergies Onetech Procédé de fractionnement d’un produit craqué obtenu par un traitement conjoint dans un craqueur catalytique à lit fluidisé d’une charge d’hydrocarbures et d’une charge d’huile issue de sources renouvelables

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4876108A (en) 1987-11-12 1989-10-24 Ensyn Engineering Associates Inc. Method of using fast pyrolysis liquids as liquid smoke
US5961786A (en) 1990-01-31 1999-10-05 Ensyn Technologies Inc. Apparatus for a circulating bed transport fast pyrolysis reactor system
US5395455A (en) 1992-03-10 1995-03-07 Energy, Mines And Resources - Canada Process for the production of anhydrosugars from lignin and cellulose containing biomass by pyrolysis
CA2638061C (en) 2006-02-09 2016-06-14 Shell Internationale Research Maatschappij B.V. Fluid catalytic cracking process
EP1892280A1 (de) * 2006-08-16 2008-02-27 BIOeCON International Holding N.V. Verfahren zum katalytischen Cracken von sauerstoffhaltigen Verbindungen
GB2447684B (en) * 2007-03-21 2011-11-23 Statoil Asa Biogasoline
US8288599B2 (en) * 2008-06-30 2012-10-16 Kior, Inc. Co-processing solid biomass in a conventional petroleum refining process unit
US20120137572A1 (en) * 2009-05-22 2012-06-07 Kior, Inc. Processing biomass with a hydrogen source
US20120304529A1 (en) * 2009-09-01 2012-12-06 Kior, Inc. Temperature-Optimized Conversion of Lignocellulosic Biomass

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2012062924A1 *

Also Published As

Publication number Publication date
CN103201357A (zh) 2013-07-10
JP2013545841A (ja) 2013-12-26
CA2816353A1 (en) 2012-05-18
BR112013011287A2 (pt) 2016-11-01
WO2012062924A1 (en) 2012-05-18

Similar Documents

Publication Publication Date Title
EP2638127A1 (de) Verfahren zur herstellung eines biokraftstoffs und/oder biochemikalie
US9169444B2 (en) Liquid fuel composition
EP2912147B1 (de) Verfahren zum katalytischen cracking eines pyrolyseöls
US20150337207A1 (en) Process for making a distillate product and/or c2-c4 olefins
US20120289752A1 (en) Process for converting a solid biomass material
US20130178672A1 (en) Process for making a distillate product and/or c2-c4 olefins
US20120271074A1 (en) Process for converting a solid biomass material
US9248444B2 (en) Process for regenerating a coked catalytic cracking catalyst
US9222031B2 (en) Suspension of solid biomass particles in a hydrocarbon-containing liquid
WO2014064008A1 (en) Process for catalytic cracking of a biomass
CN103597057B (zh) 有关产品物流分离的改进
EP2699645A1 (de) Verfahren zur umwandlung eines festen biomassematerials
WO2013160253A1 (en) Process for converting a solid biomass material
EP2699651A1 (de) Verfahren zur umwandlung eines festen biomassematerials
JP2014511938A (ja) 固体バイオマス材料を転化させる方法

Legal Events

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

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20130425

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20140103