WO2014177669A1 - Procédé pour convertir un matériau de biomasse - Google Patents

Procédé pour convertir un matériau de biomasse Download PDF

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Publication number
WO2014177669A1
WO2014177669A1 PCT/EP2014/058944 EP2014058944W WO2014177669A1 WO 2014177669 A1 WO2014177669 A1 WO 2014177669A1 EP 2014058944 W EP2014058944 W EP 2014058944W WO 2014177669 A1 WO2014177669 A1 WO 2014177669A1
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WIPO (PCT)
Prior art keywords
hydrocarbon
derived
petroleum
equal
water
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PCT/EP2014/058944
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English (en)
Inventor
Ivo Johannes DIJS
Johannes Pieter Haan
Carolus Matthias Anna Maria Mesters
Arjen Nieuwhof
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Shell Internationale Research Maatschappij B.V.
Shell Oil Company
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Application filed by Shell Internationale Research Maatschappij B.V., Shell Oil Company filed Critical Shell Internationale Research Maatschappij B.V.
Publication of WO2014177669A1 publication Critical patent/WO2014177669A1/fr

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    • 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
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • 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
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/045—Separation of insoluble materials
    • 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
    • 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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • 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
    • 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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
    • 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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/04—Dewatering
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C10L1/023—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for spark ignition
    • 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
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C10G2300/203—Naphthenic acids, TAN
    • 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
    • C10G2300/302—Viscosity
    • 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
    • C10G2300/308—Gravity, density, e.g. API
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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 a process for preparing a hydrocarbon-containing mixture, more specifically a hydrocarbon-containing mixture that is suitable for processing and/or transporting.
  • the present invention relates to a process for preparing one or more fuel components and/or one or more chemical components.
  • One alternative to easily accessible sweet crude oil are so-called disadvantaged crudes and/or unconventional petroleum deposits.
  • Disadvantaged crudes or derivatives thereof can include acidic components that contribute to the total acid number ("TAN") of the crude feed; they can have a high viscosity, contain a high level of asphaltenes and/or have a high density. Disadvantaged crudes or derivatives thereof with a relatively high viscosity and/or a relatively high density and/or a relatively high level of asphaltenes and/or a relatively high level of TAN tend to be difficult and/or expensive to transport and/or process using conventional facilities.
  • TAN total acid number
  • unconventional petroleum deposits is used for petroleum deposits that are explored by other than conventional methods.
  • Such petroleum deposits include for example bituminous sands (also sometimes referred to as oil sands or tar sands) and oil shales.
  • These petroleum deposits may for example be explored or produced via steam assisted gravity drainage (SAGD) or mining, providing mixtures of sand, water and unconventional oil.
  • SAGD steam assisted gravity drainage
  • the unconventional oil from these mixtures can have a relatively high viscosity and/or a relatively high density and/or a relatively high level of asphaltenes and/or a high content of TAN and tend to be difficult and/or expensive to transport and/or process using conventional facilities .
  • Disadvantaged crudes and/or unconventional oils may therefore sometimes be diluted with a diluent, such as for example naphtha or a condensate, before transporting and/or processing, in order to make them transportable and/or fit for processing.
  • a diluent such as for example naphtha or a condensate
  • the use of such a diluent is disadvantageous from an economic point of view, and it would be an advancement in the art to be able to reduce the amount of diluent needed or to eliminate the use of a diluent .
  • disadvantaged crudes and/or unconventional oils with a relatively high TAN may contribute to corrosion of metal components during transporting and/or processing of the disadvantaged crudes or unconventional oils.
  • Corrosion-resistant metals may be used in
  • corrosion-resistant metal often involves significant expense, and thus, the use of corrosion-resistant metal in existing equipment may not be desirable.
  • Another method to inhibit corrosion may involve addition of corrosion inhibitors to
  • disadvantaged crudes may exhibit instability during processing in conventional facilities. Such instability may result in undesired phase separation of components during transport and/or processing.
  • renewable hydrocarbon resources Another alternative to easily accessible sweet crude oil are so-called renewable hydrocarbon resources.
  • a so-called pyrolysis oil is a so-called pyrolysis oil.
  • a pyrolysis oil may suitably be produced by the pyrolysis of biomass
  • the pyrolysis product, produced by pyrolysis of a biomass comprising a lignocellulosic material may comprise hydrocarbons, oxygenated compounds, organic acids and phenolics, insoluble lignin and water.
  • the water content may amount to 25-30 wt% or even more.
  • the presence of water and oxygenated compounds in the pyrolysis oil is
  • Water may be removed by evaporation.
  • the removal of water from the pyrolysis oil via evaporation has been found to lead to the formation of a highly viscous, tar-like material and/or insolubles that may be difficult to transport and/or process.
  • the present invention provides a process comprising
  • a petroleum-derived hydrocarbon composition having a C7-asphaltenes content of equal to or more than 0.2 wt%, based on the total weight of the petroleum- derived hydrocarbon composition, which petroleum-derived hydrocarbon composition has a total acid number of equal to or more than 0.5 mg KOH/g and/or a density at 15.5°C of equal to or more than 0.8 grams/ml and/or a viscosity at 37.8°C of equal to or more than 500 centiStokes (cSt); c) mixing at least part of the biomass-derived pyrolysis product and at least part of the petroleum-derived hydrocarbon composition to produce a hydrocarbon- containing mixture;
  • the dewatered hydrocarbon-containing mixture is stable.
  • the dewatered hydrocarbon-containing mixture may further be more easily and/or more economically be transported and/or processed.
  • the dewatered hydrocarbon-containing mixture obtained in step d) may conveniently be converted via one or more hydrocarbon conversion processes into one or more fuel components and/or one or more chemical components.
  • Figure 1 illustrates three examples of a process according to the invention.
  • Figure 2 illustrates a fourth example of a process according to the invention.
  • Figure 3 illustrates a fifth example of a process according to the invention.
  • step a) of the process according to the invention a biomass material is pyrolyzed to produce a biomass- derived pyrolysis product.
  • biomass material is herein understood a composition of matter of biological origin as opposed to a composition of matter obtained or derived from petroleum, natural gas or coal. Without wishing to be bound by any kind of theory it is believed that such biomass material may contain carbon-14 isotope in an abundance of about
  • the biomass material may suitably comprise animal fat, tallow and/or solid biomass material.
  • the biomass material is a solid biomass material. More preferably the biomass material is material containing cellulose and/or lignocellulose. Such a material containing “cellulose” respectively " lignocellulose " is herein also referred to as a
  • cellulosic respectively " lignocellulosic " material.
  • a cellulosic material is herein understood a material containing cellulose and optionally also lignin and/or hemicellulose .
  • a lignocellulosic material is herein understood a material containing cellulose and lignin and optionally hemicellulose.
  • biomass materials include aquatic plants and algae, agricultural waste and/or forestry waste and/or paper waste and/or plant material obtained from domestic waste.
  • biomass materials include aquatic plants and algae, agricultural waste and/or forestry waste and/or paper waste and/or plant material obtained from domestic waste.
  • lignocellulosic material include for example agricultural wastes such as corn stover, soybean stover, corn cobs, rice straw, rice hulls, oat hulls, corn fibre, cereal straws such as wheat, barley, rye and oat straw; grasses; forestry products and/or forestry residues such as wood and wood-related materials such as sawdust and bark;
  • waste paper sugar processing residues such as bagasse and beet pulp; or mixtures thereof.
  • the solid biomass material comprises or consists of a cellulosic or lignocellulosic material selected from the group consisting of wood, sawdust, bark, straw, hay, grasses, bagasse, corn stover and/or mixtures thereof.
  • the wood may include soft wood and/or hard wood.
  • the biomass material is a solid biomass material such as for example a lignocellulosic material
  • it may suitably be washed, steam exploded, dried, roasted, torrefied and/or reduced in particle size before being pyrolyzed in step a) .
  • the biomass material is a cellulosic or lignocellulosic material it may preferably be demineralized before being pyrolyzed in step a) . During such a demineralization amongst others chloride may be removed.
  • step a) the biomass material is pyrolyzed to produce a biomass-derived pyrolysis product .
  • pyrolysis or pyrolyzing is herein understood the decomposition of the biomass material, in the presence or in the essential absence of a catalyst, at a temperature of equal to or more than 380°C.
  • pyrolysis is carried out in an oxygen- poor, preferably an oxygen-free, atmosphere.
  • an oxygen-poor atmosphere is understood an atmosphere containing equal to or less than 10 vol.% oxygen, preferably equal to or less than 5 vol.% oxygen and more preferably equal to or less than 1 vol.% oxygen.
  • an oxygen-free atmosphere is understood an atmosphere where oxygen is essentially absent. More preferably pyrolysis is carried out in an atmosphere containing equal to or less than 2 vol.% oxygen, more preferably equal to or less than 0.5 vol.% oxygen, even more preferably equal to or less than 0.1 vol. % oxygen and most preferably equal to or less than 0.05 vol.% oxygen. In a most preferred embodiment pyrolysis is carried out in the essential absence of oxygen.
  • the biomass material is preferably pyrolyzed at a pyrolysis temperature of equal to or more than 400°C, more preferably equal to or more than 450°C, even more preferably equal to or more than 500°C and most
  • the pyrolysis temperature is further preferably equal to or less than 800°C, more preferably equal to or less than 700°C and most preferably equal to or less than 650°C.
  • the pyrolysis pressure may vary widely.
  • the pyrolysis does not include an externally added catalyst.
  • the pyrolysis is a so-called catalytic pyrolysis wherein a catalyst is used.
  • suitable catalysts in such a catalytic pyrolysis include mesoporous zeolites.
  • mesoporous zeolite is herein preferably understood a zeolite containing pores with a pore diameter in the range from 2 - 50 nanometer, in line with IUPAC notation (see for example Rouquerol et al. (1994) .
  • Especially preferred catalysts for such a catalytic pyrolysis include ZSM-5 type zeolites, such as for example Zeolyst 5524G and 8014 and Albemarle UPV-2.
  • chemicals may be employed for a pretreatment of the biomass material, or catalysts may be added to the pyrolysis mixture, cf. for example, H
  • a flash pyrolysis process the biomass is rapidly heated (for example within 3 seconds) in the essential absence of oxygen to a temperature in the range of from 400 °C to 600 °C and kept at that temperature for a short period of time (for example equal to or less than 3 seconds) .
  • flash pyrolysis processes are known, for example from A. Oasmaa et al, "Fast pyrolysis of Forestry Residue 1. Effect of extractives on phase separation of pyrolysis liquids", Energy & Fuels, volume 17, number 1, 2003, pages 1-12; and A. Oasmaa et al, Fast pyrolysis bio-oils from wood and agricultural residues, Energy & Fuels, 2010, vol. 24, pages 1380-1388; US4876108;
  • a solid heating medium such as for example silica or sand.
  • the solid heating medium may for example be a fluidized solid heating medium provided in for example a fluidized bed or a riser reactor.
  • the biomass material may be fluidized within the fluidized solid heating medium and subsequently the biomass material may be pyrolysed with the heat provided by such fluidized solid heating medium.
  • any residual coke formed on the solid heating medium may be burned off to regenerate the solid heating medium.
  • the coke that is burned off may conveniently supply the heat needed to prehead the solid heating medium.
  • the pyrolyzing in step a) may be carried out in any type of pyrolysis reactor know to the person skilled in the art to be suitable for such pyrolysis process.
  • the pyrolysis reactor comprises a so-called screw reactor, wherein the biomass material is continuously conveyed through the heated reactor by means of a screw.
  • Such a reactor is sometimes also referred to as an "Auger" reactor.
  • biomass-derived pyrolysis product referred to in this invention will contain water.
  • the biomass-derived pyrolysis product may for example contain gas, solids
  • char one or more oily phase (s), and water.
  • part of the water may be present as a separate aqueous phase, whereas another part of the water may be contained within one or more oily phase (s) in a dispersed and/or emulsified form.
  • Step a) preferably further comprises separating one or more oily phase (s) containing water from the biomass- derived pyrolysis product.
  • Such one or more oily phase (s) containing water are herein also referred to as pyrolysis oil or biomass-derived pyrolysis oil.
  • the pyrolysis oil or biomass-derived pyrolysis oil referred to in this invention hence will still contain water, for example in a dispersed and/or emulsified form.
  • biomass-derived pyrolysis oil is separated from any other components (for example, gas, solids or any aqueous phase) of the biomass-derived pyrolysis product.
  • the biomass-derived pyrolysis oil can be separated from the biomass-derived pyrolysis product 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.
  • such a separation is carried out at a temperature of equal to or less than 100°C and a pressure of about 0.1 MegaPascal.
  • the biomass-derived pyrolysis product is separated in a liquid/solid separation, gas/liquid separation and/or a gas /liquid/solid separation to separate liquid biomass-derived pyrolysis product from the remainder of the biomass-derived pyrolysis product.
  • any biomass-derived pyrolysis product (also referred to as pyrolysis product vapours) or a part thereof may be at least partly condensed, for example by cooling the biomass-derived pyrolysis product.
  • a condensed liquid any residual vapours and optionally solids (such as for example any solid heating medium) may be obtained.
  • the condensation can be carried out in any manner known to be suitable therefore by the person skilled in the art. For example by means of heat- exchangers.
  • a condensation is carried out by cooling the biomass-derived pyrolysis product or part thereof with pyrolysis oil, suitably in one or more condensers, preferably in a counter-current arrangement.
  • any condensed vapours of the biomass-derived pyrolysis product may suitably be captured in such countercurrently flowing pyrolysis oil.
  • the so-obtained liquid biomass- derived pyrolysis product may contain entrained solids, such as for example the solid heating medium, that may suitably be removed by filtration thereafter.
  • the obtained liquid biomass-derived pyrolysis product preferably may consist mostly or wholly of biomass- derived pyrolysis oil. Conveniently at least part of the liquid biomass-derived pyrolysis product, preferably consisting of biomass-derived pyrolysis oil, obtained after filtration is used to condense the biomass-derived pyrolysis product gas or part thereof.
  • the part of the biomass-derived pyrolysis product that is liquid may comprise one or more oily phase (s) and optionally an aqueous phase.
  • the part of the biomass-derived pyrolysis product that is liquid may also consist of one or more oily phase (s) comprising dispersed and/or emulsified water therein.
  • oily phase (s) are herein referred to as
  • any aqueous phase is present in the liquid biomass-derived pyrolysis product, such aqueous phase may or may not be separated from the one or more oily phases. If separated, the aqueous phase may be separated from the biomass-derived pyrolysis oil in for example a water/oil phase separation step. However, even after such a water/oil phase separation step,
  • the biomass-derived pyrolysis oil in the process of the invention may include for example carbohydrates, olefins, paraffins, oxygenates and residual water.
  • an oxygenate is herein understood a compound containing carbon, hydrogen and oxygen.
  • the oxygenates may for example include aldehydes, carboxylic acids, ethers, esters, alkanols, phenols and ketones.
  • the biomass-derived pyrolysis oil, or mixture of biomass-derived pyrolysis oil and aqueous phase may suitably comprise water in an amount equal to or more than 0.1 wt%, preferably equal to or more than lwt%, more preferably equal to or more than 2 wt%, even more preferably equal to or more than 5 wt%, still more preferably equal to or more than 10 wt% and most
  • biomass-derived pyrolysis oil or mixture of biomass-derived pyrolysis oil and aqueous phase may suitable comprise in the range from 1 to 55 wt%, more suitably in the range from 10 to 45 wt%, most suitably in the range from 15 to 35 wt%, based on the total weight of the biomass-derived pyrolysis oil, respectively the total weight of biomass-derived pyrolysis oil and aqueous phase .
  • the Total Acid Number of the biomass- derived pyrolysis oil may be at most 250 mg KOH/g, more preferably in the range of from 1 mg KOH/g to
  • water content is as measured by ASTM E203 and Total acid number is as measured by using ASTM D664.
  • step a) may comprise dimineralizing the biomass-derived pyrolysis product or part thereof (such as the biomass-derived pyrolysis oil) , for example before forwarding to step c) . During such a demineralization amongst others chloride may be removed.
  • step a) may therefore further comprise the removal of minerals such as chloride from the biomass material before pyrolyzing and/or the removal of minerals such as chloride from the biomass-derived pyrolysis product after pyrolyzing.
  • the biomass-derived pyrolysis product obtained in step a) or part thereof may be forwarded directly or indirectly to step c) .
  • a biomass-derived pyrolysis oil is forwarded directly or indirectly to step c) .
  • the biomass-derived pyrolysis product or part thereof (such as the biomass-derived pyrolysis oil) may first be stored for a period "t" before forwarding.
  • step b) a petroleum-derived hydrocarbon
  • composition having a C7-asphaltenes content of equal to or more than 0.2 wt%, based on the total weight of the petroleum-derived hydrocarbon composition, which petroleum-derived hydrocarbon composition has a total acid number of equal to or more than 0.5 mg KOH/g and/or a density at 15.5°C of equal to or more than 0.8 grams/ml and/or a viscosity at 37.8°C of equal to or more than 500 centiStokes (cSt) .
  • cSt centiStokes
  • the petroleum-derived hydrocarbon composition as mentioned in step b) may preferably be a so-called extra heavy oil.
  • the petroleum-derived hydrocarbon composition may comprise one or more hydrocarbon compounds and preferably comprises two or more hydrocarbon compounds.
  • a hydrocarbon compound is herein understood a compound containing hydrogen and carbon. Such hydrocarbon compound may further contain heteroatoms such as oxygen, sulphur and/or nitrogen.
  • the petroleum-derived hydrocarbon composition may also comprise hydrocarbon compounds consisting of only hydrogen and carbon.
  • the petroleum-derived hydrocarbon composition is preferably a petroleum-derived hydrocarbon composition that has a Total Acid Number (TAN) of equal to or more than 1.0 mg KOH/g, more preferably equal to or more than
  • the petroleum-derived hydrocarbon composition can have a TAN of equal to or more than 7.0 mg KOH/gram.
  • the TAN of the petroleum-derived hydrocarbon composition is preferably equal to or less than 100 mg KOH/g, more preferably equal to or less than 50 mg KOH/g and most preferably equal to or less than 10 mg KOH/g.
  • the petroleum-derived hydrocarbon composition preferably has a C7-asphaltene content of equal to or more than 0.5wt%. More preferably, the C7-asphaltenes content of the petroleum-derived hydrocarbon composition may be equal to or more than 0.7 %wt, still more
  • the CI - asphaltenes content is in the range of from 0.9 to 15 %wt or in the range of from 2.0 to 15 %wt based on the total weight of the petroleum-derived hydrocarbon composition.
  • asphaltenes content or C7-asphaltenes content is as determined by IP143, using n-heptane as a solvent .
  • the petroleum-derived hydrocarbon composition may have a kinematic viscosity at 37.8°C as determined using
  • centistokes preferably of equal to or more than 1000 centistokes; more preferably of equal to or more than 4000 centistokes; even more preferably of equal to or more than 5000 centistokes and most preferably of equal to or more than 8000 centistokes.
  • the petroleum-derived hydrocarbon composition may have a kinematic viscosity at 37.8 °C as determined using ASTM Method D445 of equal to or less than 40000 centistokes.
  • the petroleum-derived hydrocarbon composition can even have a kinematic viscosity at 100°C of equal to or more than 5 centistokes, possibly even equal to or more than 50 centistokes, equal to or more than 100 or even equal to or more than 200 centistokes.
  • a preferred kinematic viscosity at 100°C of equal to or more than 5 centistokes, possibly even equal to or more than 50 centistokes, equal to or more than 100 or even equal to or more than 200 centistokes.
  • the petroleum-derived hydrocarbon composition has a kinematic viscosity at 100°C of equal to or less than 3000 centistokes.
  • the petroleum-derived hydrocarbon composition preferably has a density at 15.5°C of equal to or more than 0.9 grams/ml; more preferably equal to or more than 1.0 grams/ml. In some embodiments the petroleum-derived hydrocarbon composition may have a density of equal to or less than 1.3 grams/ml.
  • the total petroleum-derived hydrocarbon composition has a boiling point equal to or higher than 95°C, more preferably equal to or higher than 200°C, even more preferably equal to or higher than 300°C and most preferably equal to or more than 400 °C.
  • the petroleum-derived hydrocarbon composition has an initial atmospheric boiling point of equal to or more than 130 °C .
  • the initial atmospheric boiling point of the petroleum-derived hydrocarbon composition is equal to or more than 150 °C, more preferably equal to or more than 180 °C .
  • the atmospheric boiling point range of the petroleum-derived hydrocarbon composition may be from 220 °C to 800 °C, more preferably from 300 °C to 700 °C.
  • the hydrogen to carbon weight ratio (H/C ratio) of the petroleum-derived hydrocarbon composition may be at most 0.15 w/w, more preferably in the range of from 0.1 to 0.14 w/w, even more preferably in the range of from 0.11 to 0.13 w/w.
  • boiling point is the atmospheric boiling point, unless indicated otherwise, with the atmospheric boiling point being the boiling point as determined at a pressure of 100 kiloPascal (i.e. 0.1 MegaPascal) .
  • initial boiling point and boiling point range of the high boiling hydrocarbon mixtures are as determined by ASTM D2887.
  • pressure is absolute pressure.
  • H/C ratio is as determined by ASTM D5291.
  • asphaltenes content or CI - asphaltenes content is as determined by IP143, using n- heptane as a solvent .
  • the petroleum-derived hydrocarbon composition is a so-called crude, also sometimes referred to as crude oil.
  • a crude is herein understood a petroleum-derived hydrocarbon composition that has not been processed yet.
  • a crude may be understood a petroleum-derived hydrocarbon composition that has not been distilled and/or
  • distributions for example, naphtha, distillates, VGO, and/or lubricating oils.
  • the petroleum-derived hydrocarbon may for example be a whole crude, topped crude, desalted crude, desalted topped crude or combinations thereof.
  • Topicped refers to a rude that has been treated such that at least some of the components that have a low boiling point (for example a boiling point below 35 °C at 0.101 MPa) have been removed .
  • the petroleum-derived hydrocarbon composition is a disadvantaged crude or is derived from a disadvantaged crude.
  • disadvantaged crudes include, but are not limited to, crudes from of the following regions of the world: U.S. Gulf Coast and southern California, Canada Tar sands, Brazilian Santos and Campos basins, Egyptian Gulf of Suez, Chad, United Kingdom North Sea, Angola Offshore, Chinese Bohai Bay, Venezuelan Zulia, Malaysia, and Indonesia Sumatra.
  • the petroleum- derived hydrocarbon composition may be obtained from or derived from a so-called unconventional petroleum deposit.
  • the petroleum-derived hydrocarbon composition may comprise an unconventional oil or a derivative thereof.
  • the petroleum-derived hydrocarbon composition may comprise or consist of bitumen. More preferably the petroleum-derived
  • hydrocarbon composition may be obtained from or derived from so-called bituminous sands, also referred to as oil sands or tar sands .
  • the petroleum-derived hydrocarbon composition can be a petroleum derived hydrocarbon composition containing hydrocarbon compounds and water.
  • the petroleum-derived hydrocarbon composition may comprise equal to or more than 0.5 wt% water, equal to or more than 1.0 wt% water or even equal to or more than 5.0 wt% water, based on the total weight of such petroleum-derived hydrocarbon composition.
  • the petroleum-derived hydrocarbon composition may contain hydrocarbon compounds, water and sand.
  • the petroleum-derived hydrocarbon composition may for example contain in the range from 0.1 to 99.9 wt% hydrocarbon compounds and in the range from 0.1 to 99.9 wt% sand and/or water, based on the total weight of the petroleum-derived hydrocarbon composition.
  • composition may comprise bitumen, which bitumen may for example be supplied as a mixture of bitumen, water and sand.
  • bitumen may for example be supplied as a mixture of bitumen, water and sand.
  • Such a mixture of bitumen, water and sand may for example contain in the range from 5wt% to 50wt%,
  • the mud may consist of water and sand, and may contain in the range of 5wt% to 50wt%, preferably in the range from 10wt% to 30 wt% of water; and for example in the range from 50wt% to 95wt%, preferably in the range from 70wt% to 90wt% of sand, based on the total weight of the mud.
  • the petroleum-derived hydrocarbon composition may preferably comprise equal to or more than 33.3 wt% hydrocarbon compounds, more preferably equal to or more than 60wt% hydrocarbon compounds and still more preferably equal to or more than
  • such a petroleum-derived hydrocarbon composition may comprise equal to or less than 99 wt% hydrocarbon compounds, based on the total weight of the petroleum-derived hydrocarbon composition.
  • the petroleum-derived hydrocarbon composition may further comprise equal to or less than 33.3 wt% water, more preferably equal to or less than 10wt% water and most preferably equal to or less than 5wt% water, based on the total weight of the petroleum-derived hydrocarbon composition.
  • such a petroleum-derived hydrocarbon composition may comprise equal to or more than 0.5 wt% water, based on the total weight of the petroleum-derived hydrocarbon composition.
  • the petroleum-derived hydrocarbon composition may further comprise equal to or less than 33.3 wt% sand, more preferably equal to or less than 10wt% sand and most preferably equal to or less than 5wt% sand, based on the total weight of the petroleum-derived hydrocarbon composition.
  • a petroleum-derived hydrocarbon composition may comprise equal to or more than 0.5 wt% sand, based on the total weight of the petroleum-derived hydrocarbon composition.
  • step c) at least part of the biomass-derived pyrolysis product containing water and at least part of the petroleum-derived hydrocarbon composition are mixed to produce a hydrocarbon-containing mixture containing water .
  • the "at least part of the biomass-derived pyrolysis product" is a biomass-derived pyrolysis oil as described herein above. As explained above, such biomass- derived pyrolysis oil still contains water.
  • the mixture of at least part of the biomass-derived pyrolysis product (for example the biomass-derived pyrolysis oil) and at least part of the petroleum-derived hydrocarbon composition can be produced in any manner known to the skilled person in the art.
  • the part or whole of the biomass-derived pyrolysis product may be added to part or whole of the petroleum-derived hydrocarbon composition, or the petroleum-derived hydrocarbon composition may be added to part or whole of the
  • pyrolysis product or part thereof and the petroleum- derived hydrocarbon composition may be brought together, for example by in-line blending or within a static mixer.
  • the part or whole of the pyrolysis product and the part or whole of the petroleum-derived hydrocarbon composition may be mixed, for example by means of a mixer or via one or more baffles, preferably in an in-line mixer or static mixer.
  • such biomas s-derived pyrolysis oil and the part or whole of the petroleum-derived hydrocarbon composition may be mixed in a weight ratio of biomass- derived pyrolysis oil to petroleum-derived hydrocarbon composition (grams biomass-derived pyrolysis oil/grams petroleum-derived hydrocarbon composition) of at least 0.5/99.5, more preferably at least 1/99, still more preferably at least 2/98, and even still more preferably at least 5/95, respectively.
  • hydrocarbon composition may be mixed in a weight ratio of biomass-derived pyrolysis oil to petroleum-derived hydrocarbon composition (grams biomass-derived pyrolysis oil/grams petroleum-derived hydrocarbon composition) of at most 75/25, more preferably at most 70/30, even more preferably at most 60/40, and most preferably at most 50/50 respectively.
  • the petroleum-derived hydrocarbon composition may be mixed in a weight ratio of biomass-derived pyrolysis oil to petroleum-derived hydrocarbon composition (grams biomass-derived pyrolysis oil/grams petroleum-derived hydrocarbon composition) in the range from 1/99 to 30/70, more preferably in the range from 5/95 to 25/75, most preferably in the range from 10/90 to 20/80.
  • Step c) results in a hydrocarbon-containing mixture being produced.
  • This hydrocarbon-containing mixture produced in step c) will still contain water, for example in a dispersed or emulsified form.
  • step d) of the process according to the present invention the hydrocarbon-containing mixture is dewatered to produce a dewatered hydrocarbon-containing mixture.
  • Dewatering can be carried out in any manner known by the person skilled in the art to be suitable for the removal of water from a hydrocarbon-containing mixture.
  • Dewatering of the hydrocarbon-containing mixture may for example be carried out by evaporating of the water; membrane separation; phase separation; absorption or adsorption of the water; and/or any combination thereof.
  • the dewatering may be carried out in a continuous operation or as a batch operation.
  • the hydrocarbon-containing mixture is dewatered by means of evaporation.
  • Evaporation of the water, and optionally any volatile acids, from the hydrocarbon-containing mixture may for example be achieved by flashing or distillation of the hydrocarbon- containing mixture .
  • the water may be evaporated from the hydrocarbon-containing mixture in one or more wipe-film evaporators connected in series.
  • water, and optionally any volatile acids are evaporated from the hydrocarbon- containing mixture by flashing of such hydrocarbon- containing mixture.
  • the flashing may for example be carried out by feeding a hydrocarbon-containing mixture under a pressure for example in the range from 200 to 1000 KiloPascal (KPa) into a flash vessel operated at a pressure for example in the range from 0.1 to 50 KPa at for example a temperature in the range from 90 to 150°C.
  • a distillation apparatus having a separation column may be selected to evaporate the water.
  • the distillation apparatus and the conditions of operating the distillation apparatus are selected such that water is evaporated and condensed as a water rich distillate fraction, and higher boiling hydrocarbon compounds (for example hydrocarbon compounds boiling at a temperature of equal to or more than 100°C, preferably at a temperature of equal to or more than
  • the bottom temperature is selected such that the bottom fraction is sufficiently low in
  • the temperature in the range of from 50 °C to 200 °C may be selected, more suitable in the range of from 80 °C to 150 °C .
  • the pressure may suitably be selected in the range of from 0.01 kPa to 500 kPa, more suitably in the range of from 0.1 kPa to 120 kPa, preferably in the range of from 0.2 kPa to 60 kPa and more preferably in the range of from 0.2 kPa to 10 kPa (kiloPascal) .
  • the higher boiling hydrocarbon compounds have been defined hereinbefore by its atmospheric boiling point (i.e. at a pressure of 0.1 MegaPascal, the skilled person will appreciate that the atmospheric boiling point is specified such that a distillation apparatus can be operated at a pressure other than atmospheric pressure
  • Such bottom fraction can suitable be used as a dewatered hydrocarbon-containing mixture, in the next steps of the process according to this invention.
  • step d) preferably equal to or more than 1 wt% of the total weight of water in the hydrocarbon-containing mixture is removed, more preferably equal to or more than 10 wt%, even more preferably equal to or more than 50wt%, still more preferably equal to or more than 70wt% and most preferably equal to or more than 90 wt% of the total weight of water in the hydrocarbon-containing mixture is removed.
  • Dewatering of the hydrocarbon-containing mixture may preferably be effected to the extent that a dewatered hydrocarbon-containing mixture is obtained.
  • dewatered hydrocarbon-containing mixture may have a water content of at most 5 %wt, more preferably at most 2 %wt, preferably at most 1 %wt, based on the total weight of the dewatered hydrocarbon-containing mixture.
  • the water content of the dewatered hydrocarbon-containing mixture obtained may be at least 0.001 %wt, or at least 0.01 %wt, based on the total weight of the dewatered hydrocarbon-containing mixture .
  • the process according to the invention may especially be advantageous when transporting or processing a so-called unconventional oil obtained from an unconventional petroleum deposit. As mentioned above, such
  • unconventional oil may sometimes be diluted with a diluent, such as for example naphtha, before transporting and/or processing.
  • a diluent such as for example naphtha
  • bituminous sand for example a mixture of 70wt% sand, 10wt% water and 20wt% bitumen, is obtained from a tar sand production side.
  • bituminous sand (102) is diluted with a stream of naphtha (104) and forwarded to a separator (106), where a hydrocarbon-containing stream (108) is separated from a water-containing stream (110) and a sand-containing stream (112) .
  • the water-containing stream (110) and sand- containing stream (112) may optionally be removed simultaneously as one mud stream (not shown) .
  • the hydrocarbon-containing stream (108) is subsequently forwarded to a flasher or distillation vessel (114), where a gaseous fraction (116), a naphtha-containing fraction (118) and a bitumen-containing fraction (120) are separated.
  • At least part of the naphtha-containing fraction (118) may conveniently be recycled and used as a stream of naphtha (104) for dilution.
  • a biomass-derived, water-containing pyrolysis oil as described herein may advantageously be used to partly or wholly replace the stream of naphtha diluent (104) as illustrated by stream (122); be added to the hydrocarbon- containing stream (108) as illustrated by stream (124); and/or be added to the bitumen containing fraction (120) as illustrated by stream (126) .
  • the process according to this invention can advantageously comprise
  • the petroleum-derived hydrocarbon composition for this embodiment contains bitumen, water and sand.
  • the process according to this embodiment advantageously allows one to remove water contained in the water-containing pyrolysis product and water contained in the petroleum-derived hydrocarbon composition simultaneously. This may
  • process according to this embodiment could advantageously allow one to remove part of the acids from both the pyrolysis oil as well as from the petroleum-derived hydrocarbon composition.
  • the dewatering may suitably be carried out in one or more steps.
  • the hydrocarbon-containing mixture may be dewatered by separating an aqueous phase in a phase separation in a first step optionally followed by removing any remaining or residual water by means of evaporation in a second step.
  • the phase separation may suitably further include a gas/liquid, solids/liquid and/or gas/solids/liquid phase separation to remove any solids and/or gases that may be contained in the
  • FIG. 1 An example of such an embodiment is illustrated by figure 1, where a stream of biomass-derived water- containing pyrolysis product (122) partly or wholly replaces the stream of naphtha diluent (104) .
  • water from the biomass-derived water- containing pyrolysis product (122) and water from the petroleum-derived hydrocarbon composition (102) may simultaneously be removed in separator (106), whereafter any remaining or residual water may conveniently be removed in flasher or distillation vessel (114) .
  • the process according to the invention may comprise
  • the petroleum-derived hydrocarbon composition for this embodiment contains bitumen, water and sand.
  • An example of such an embodiment is illustrated by figure 1, where a stream of biomass-derived water-containing pyrolysis product (126) is added to a bitumen-containing fraction (120) obtained from the flasher or distillation vessel (114) .
  • a disadvantage of this second embodiment is that after the stream of biomass-derived water-containing pyrolysis product (126) is added to the bitumen- containing fraction (120) a water-containing hydrocarbon- containing mixture is obtained and an optional additional dewatering unit (140, in dotted lines), such as an additional flasher or distillation vessel, may be needed to dewater the water-containing hydrocarbon containing mixture .
  • the process according to the invention may comprise
  • composition by means of phase separation to produce a petroleum-derived hydrocarbon composition comprising residual water;
  • the petroleum derived hydrocarbon composition in step b) of this third embodiment comprises bitumeninous sand (i.e.b itumen, sand and water) and a diluent such as naphtha.
  • bitumeninous sand i.e.b itumen, sand and water
  • a diluent such as naphtha
  • bituminous sand for example a mixture of about 80wt% inorganic solids (such as for example sand, clays and minerals), about 10wt% water and about 10wt% bitumen, is obtained from a tar sand
  • This stream of bituminous sand (202) is diluted with a stream of water (204) and forwarded to a separator (206) .
  • froth (208) is obtained from the separator (206) a stream of froth (208) is obtained.
  • Such stream of froth (208) may for example contain about 33wt% to 40wt% bitumen, about 33wt% to 40wt% water, and about 20wt% to
  • inorganic solids for example mainly clays
  • waste stream (210) comprising for example sand and water (sometimes referred to as mud) is obtained from separator (206) .
  • a biomass material (222), for example wood, is pretreated in pretreatment unit (224), where it may suitably be washed, demineralized, steam exploded, dried, roasted, torrefied and/or reduced in particle size.
  • the pretreated biomass material (226) is
  • the obtained water-containing biomass-derived pyrolysis product (230) is subsequently phase separated in a separation unit (232) to remove gases and solids and obtain a liquid biomass-derived pyrolysis product (234) containing biomass-derived pyrolysis oil and water.
  • the liquid biomass-derived pyrolysis product (234) is mixed with the stream of froth (208) derived from the
  • bituminous sand (202) bituminous sand (202) .
  • the liquid biomass-derived pyrolysis product (234) and the stream of froth (208) are subsequently supplied as one water-containing
  • hydrocarbon-containing mixture (236) to a washing vessel (214) .
  • the water-containing hydrocarbon-containing mixture (236) which may still be in the form of a froth, is washed with a stream of naphtha (216) .
  • the naphtha may partly be recycled naphtha from stream (247) and partly fresh naphtha from stream (217) .
  • an waste stream comprising water (218) and a product stream comprising naphtha and bitumen (220) are retrieved.
  • the product stream comprising naphtha and bitumen (220) is suitably subsequently forwarded to a hot stripper (240) .
  • a stream comprising naphtha (242), a stream comprising water (244) and a stream comprising bitumen (246) are obtained.
  • the stream of naphtha (242) may suitably be at least partly (247) recycled to washing vessel (214) .
  • part of the stream of naphtha (248) may optionally be used to dilute the stream of bitumen (246) .
  • water obtained from streams (210) and/or (218) and/or (244) may be conveniently recycled and reused as water in stream (204) .
  • Such a disadvantaged crude may sometimes be diluted with a diluent, such as for example a condensate, before transporting and/or processing.
  • a diluent such as for example a condensate
  • a disadvantaged crude (302) for example a mixture of 10 wt% sand, 10 wt% water and 80 wt% bitumen, is obtained from a SAGD production side.
  • This stream of disadvantaged crude (302) is diluted with a stream of condensate (304) and forwarded to a standard
  • electrostatic precipitator to wash the oil with water and remove any salts (306) .
  • a hydrocarbon-containing stream (308) is separated from a stream containing water and sand (310) .
  • the hydrocarbon-containing stream (308) can subsequently be transported or pipelined to a refinery.
  • biomass-derived pyrolysis oil as described herein may advantageously be used to partly or wholly replace the stream of condensate diluent (304) as illustrated by stream (322); or be added to the
  • hydrocarbon-containing stream (308) as illustrated by stream (324) .
  • stream (324) hydrocarbon-containing stream
  • the obtained hydrocarbon-containing mixture may be forwarded to a flasher or distillation vessel (314), where a water-containing fraction (318) and a dewatered hydrocarbon-containing mixture (320) can be separated.
  • the flasher or distillation vessel (314) may conveniently be located at the SAGD production location or at a refinery.
  • the dewatered hydrocarbon-containing mixture obtained in step d) may suitably be more easy and/or more economic to process and/or transport.
  • the transportability and/or processibility of the dewatered hydrocarbon-containing mixture may even be further improved by upgrading the dewatered hydrocarbon- containing mixture in one or more hydrocarbon upgrading processes .
  • step d) therefore further comprises converting the dewatered hydrocarbon-containing mixture in one or more hydrocarbon upgrading processes to produce an upgraded dewatered hydrocarbon-containing mixture .
  • Such one or more hydrocarbon upgrading processes preferably comprise contacting the dewatered hydrocarbon- containing mixture with hydrogen in the presence of a catalyst to produce an upgraded dewatered hydrocarbon- containing mixture.
  • a catalyst is preferably a hydrotreatment catalyst as described in more detail below.
  • the one or more hydrocarbon upgrading processes may be carried out at a temperature in the range from 250 to 550°C and a hydrogen partial pressure in the range from 1.0 to 10.0 MPa.
  • the hydrocarbon upgrading process may suitably be carried out in a fixed bed or in a moving bed, such as an ebullated bed or riser reactor .
  • LC-FINER LC-FINER
  • hydrocarbon mixtures (152) and (252) hydrocarbon mixtures (152) and (252) .
  • The, optionally upgraded, dewatered hydrocarbon- containing mixture may suitably be converted via one or more hydrocarbon conversion processes into one or more fuel components and/or one or more chemical components.
  • the invention hence also provides a process for producing one or more fuel components and/or one or more chemical components comprising
  • a petroleum-derived hydrocarbon composition having a C7-asphaltenes content of equal to or more than 0.2 wt%, based on the total weight of the petroleum- derived hydrocarbon composition, which petroleum-derived hydrocarbon composition has a total acid number of equal to or more than 0.5 mg KOH/g and/or a density at 15.5°C of equal to or more than 0.8 grams/ml and/or a viscosity at 37.8°C of equal to or more than 500 centiStokes (cSt) r
  • hydrocarbon conversion processes into one or more fuel components and/or one or more chemical components.
  • the dewatered hydrocarbon-containing mixture or upgraded dewatered hydrocarbon-containing mixture obtained in step d) or part thereof may first be stored for a period "t" before forwarding.
  • a period "t” may preferably lie in the range from 1 hour to 1 month.
  • Step e) may for example include a fluid catalytic cracking process, a hydrocracking process, a thermal cracking process, a hydro-isomerization process, a hydro- desulphurization process or any combination thereof.
  • step e) comprises a
  • hydrotreatment of the dewatered hydrocarbon-containing mixture may for example comprise a hydrogenation, hydrodeoxygenation, hydrocracking, hydroisomerization or any combination thereof.
  • step e) comprises a hydrocracking step, wherein the dewatered hydrocarbon- containing mixture is contacted with hydrogen in one or more moving bed reactors comprising a catalyst at a temperature in the range from 350 to 500°C to produce a reaction product comprising one or more cracked products.
  • the catalyst is preferably a hydrotreatment catalyst comprising one or more metals of group VIII of the periodic table and/or one or more metals metal of group VIB of the periodic table.
  • the catalyst may comprise a metal selected from the group comprising nickel, palladium, molybdenum, tungsten, platinum, cobalt, rhenium and/or ruthenium.
  • the catalyst is a nickel/tungsten comprising catalyst, a nickel/molybdenum comprising catalyst, cobalt/tungsten comprising catalyst or cobalt/molybdenum comprising catalyst.
  • the above mentioned metals may be present in an alloy or oxide form.
  • the catalyst further comprises a support, which may be used to carry the metal or metals.
  • a support which may be used to carry the metal or metals.
  • Such a catalyst comprising one or more metals on a support is herein also referred to as heterogeneous catalyst.
  • suitable supports include alumina, silica, silica-alumina, zirconia, titania, and/or mixtures thereof.
  • the support may comprise a zeolite, but preferably comprises amorphous alumina, silica or silica- alumina .
  • the catalyst comprises one or more oxides of molybdenum, cobalt, nickel and/or tungsten on a carrier comprising amorphous alumina, silica or silica- alumina .
  • the catalyst may be prepared in any manner known to be suitable by the person skilled in the art.
  • the catalyst is a so-called extruded catalyst, prepared by extrusion of its
  • the catalyst is a sulfided catalyst.
  • the catalyst may be sulfided in-situ or ex- situ .
  • the catalyst is sulfided in-situ or its sulfidation is maintained in-situ by contacting it with a stream of hydrogen that comprises hydrogensulfide, for example a stream of hydrogen that contains in the range from 0.1 to 10wt% hydrogensulfide based on the total weight of the stream of hydrogen.
  • a colloidal or dispersed catalyst may be used.
  • a colloidal or dispersed catalyst may be formed in-situ by mixing one or more catalyst precursors in the feed in such a manner that a colloidal or dispersed catalyst is formed within the one or more moving bed reactors .
  • step e) comprises a hydrocracking step, a fluid catalytic cracking step and/or a thermal catalytic cracking step a reaction product is produced comprising one or more cracked products .
  • a cracked product is herein understood a product comprising one or more compounds obtained by cracking of one or more larger compounds .
  • the reaction product or part thereof is subsequently fractionated to produce one or more product fractions .
  • a product fraction boiling in the gasoline range for example from about 35°C to about 210°C
  • a product fraction boiling in the diesel range for example from about 210°C to about 370°C
  • a product fraction boiling in the vacuum gas oil range for example from about 370°C to about 540°C
  • a short residue product fraction for example boiling above 540°C
  • Any one or more product fractions obtained by fractionation may or may not be further hydrotreated or hydroisomerized to obtain a hydrotreated or
  • The, optionally hydrotreated or hydroisomerized, product fraction (s) may be used as biofuel and/or biochemical component (s) .
  • one or more product fractions produced in the fractionation can be blended as a biofuel component and/or a biochemical component with one or more other components to produce a biofuel and/or a biochemical.
  • a biofuel respectively a biochemical is herein understood a fuel or a chemical that is at least party derived from a renewable energy source.
  • Examples of one or more other components with which the, optionally hydrotreated or hydroisomerized, one or more product fractions may be blended include anti- oxidants, corrosion inhibitors, ashless detergents, dehazers, dyes, lubricity improvers and/or mineral fuel components, but also conventional petroleum derived gasoline, diesel and/or kerosene fractions.
  • the invention can further be illustrated by the following non-limiting examples.
  • the Peace River bitumen had a Total Acid Number of about 4-5 mg KOH/g and a C7-asphaltene content of about 10.9 wt%.
  • the resultant mixture was placed in a round-bottom flask of a standard laboratory rotary evaporator. After attaching the flask to the rotary evaporator, an oil bath was placed around the flask and heated to 110 °C, while the flask was allowed to rotate.

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  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
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Abstract

La présente invention concerne un procédé comprenant a) la pyrolyse d'un matériau de biomasse pour produire un produit de pyrolyse dérivé de biomasse ; b) la production d'une composition d'hydrocarbures dérivée de pétrole ayant une teneur en asphaltènes en C7 supérieure ou égale à 0,2 % en poids, sur la base du poids total de la composition d'hydrocarbures dérivée de pétrole, ladite composition d'hydrocarbures dérivée de pétrole ayant un indice d'acide total supérieur ou égal à 0,5 mg KOH/g et/ou une masse volumique à 15,5 °C supérieure ou égale à 0,8 gramme/ml et/ou une viscosité à 37,8 °C supérieure ou égale à 500 centiStokes (cSt) ; c) le mélange d'au moins une partie du produit de pyrolyse dérivé de biomasse et au moins une partie de la composition d'hydrocarbures dérivée de pétrole pour produire un mélange contenant des hydrocarbures ; d) la déshydratation du mélange contenant des hydrocarbures pour produire un mélange contenant des hydrocarbures déshydraté.
PCT/EP2014/058944 2013-05-02 2014-05-01 Procédé pour convertir un matériau de biomasse WO2014177669A1 (fr)

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CA2941568A1 (fr) 2015-08-31 2017-02-28 University Of New Brunswick Procede de valorisation de liquides d'hydrocarbure lourd
EP4100491A1 (fr) * 2020-02-05 2022-12-14 Preem Aktiebolag Hydrocraquage en suspension d'huile de pyrolyse et charge d'alimentation hydrocarbonée, telle qu'une charge d'alimentation dérivée du pétrole

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999010452A1 (fr) * 1997-08-29 1999-03-04 Exxon Research And Engineering Company Procede thermique de reduction de l'indice d'acidite total du petrole brut
US5882506A (en) * 1997-11-19 1999-03-16 Ohsol; Ernest O. Process for recovering high quality oil from refinery waste emulsions
US6007702A (en) * 1998-05-22 1999-12-28 Texaco Inc. Process for removing water from heavy crude oil
WO2009146225A1 (fr) * 2008-05-30 2009-12-03 Uop Llc Hydroconversion en phase boue de charges de départ biorenouvelables
WO2012035410A2 (fr) * 2010-09-14 2012-03-22 IFP Energies Nouvelles Procédés de valorisation d'huile biologique en hydrocarbures de transport
WO2013064563A1 (fr) * 2011-10-31 2013-05-10 Shell Internationale Research Maatschappij B.V. Procédé pour la valorisation d'une huile, produit combustible et fraction de produits hydrocarbonés

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999010452A1 (fr) * 1997-08-29 1999-03-04 Exxon Research And Engineering Company Procede thermique de reduction de l'indice d'acidite total du petrole brut
US5882506A (en) * 1997-11-19 1999-03-16 Ohsol; Ernest O. Process for recovering high quality oil from refinery waste emulsions
US6007702A (en) * 1998-05-22 1999-12-28 Texaco Inc. Process for removing water from heavy crude oil
WO2009146225A1 (fr) * 2008-05-30 2009-12-03 Uop Llc Hydroconversion en phase boue de charges de départ biorenouvelables
WO2012035410A2 (fr) * 2010-09-14 2012-03-22 IFP Energies Nouvelles Procédés de valorisation d'huile biologique en hydrocarbures de transport
WO2013064563A1 (fr) * 2011-10-31 2013-05-10 Shell Internationale Research Maatschappij B.V. Procédé pour la valorisation d'une huile, produit combustible et fraction de produits hydrocarbonés

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