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WO2025132804A1 - Procédé de préparation de monoxyde de carbone (co) et d'hydrogène moléculaire (h2) - Google Patents

Procédé de préparation de monoxyde de carbone (co) et d'hydrogène moléculaire (h2) Download PDF

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Publication number
WO2025132804A1
WO2025132804A1 PCT/EP2024/087425 EP2024087425W WO2025132804A1 WO 2025132804 A1 WO2025132804 A1 WO 2025132804A1 EP 2024087425 W EP2024087425 W EP 2024087425W WO 2025132804 A1 WO2025132804 A1 WO 2025132804A1
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obtaining
subjecting
composite material
optionally
accordance
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Inventor
Indre THIEL
Michael Henningsen
Andre BADER
Simon Wachter
Jonas Matthias MAIRHOFER
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • 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
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/049—Composition of the impurity the impurity being carbon
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • C01B2203/147—Three or more purification steps in series

Definitions

  • the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a pyrolysis oil, in particular from a composite material such as wind turbine blades.
  • the present invention further relates to recycling processes.
  • Composite materials such as wind turbine blades, typically comprise a matrix and a fiber component as well as various other components such as adhesives and coatings. Due to their complex composition, they are difficult to recycle. For example, end-of-life wind turbine blades are frequently used for landfill or are incinerated, which are not the best solutions in view of carbon footprint. Therefore, there is the need to provide improved processes for the treatment of waste, in particular composite materials, in order to render the use of such composite material more sustainable. Among others, there is the need to efficiently recycle carbon containing material.
  • the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H 2 ), the process comprising: a) providing a feed stream F1 comprising a pyrolysis oil; subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally steam, into a POx reactor being operated at a temperature above 400 °C and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the steam, into said reactor, obtaining a raw gas stream S1 comprising in addition to CO and H 2 , CO 2 , H 2 O, CH4, solid particulates and optionally H 2 S; b) subjecting S1 obtained in accordance with a) to a first purification stage, obtaining a purified gas stream S2 comprising CO, H2 and CH4, S2 being depleted in CO2, H2O and solid particulates compared to S1 , the first purification stage comprising: b-1
  • the pyrolysis oil used in a) can originate from any solid material, preferably a composite material, such as (end-of-life) wind turbine blade or parts thereof.
  • the present invention further relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a composite material, the process comprising: a) providing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining the stream F1 comprising the pyrolysis oil; subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally steam, into a POx reactor being operated at a temperature above 400 °C and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the steam, into said reactor, obtaining a raw gas stream S1 comprising in addition to CO and H 2 , CO2, H2O, CH4, solid particulates and optionally H2S; b) subjecting S1 obtained in accordance with a) to a first purification stage, obtaining a purifier
  • the present invention relates to a process for preparing CO and H 2 from a composite material, the process comprising: a) providing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining a pyrolysis oil, and optionally adding a further material, obtaining the stream F1 comprising the pyrolysis oil and optionally the further material; and subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally one or more of steam and CO 2 , into a POx reactor being operated at a temperature above 400 °C, and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the one or more of steam and CO 2 , in said reactor, obtaining a raw gas stream S1 comprising CO and H 2 and additionally CO 2 , H 2 O, CH4, solid particulates and optionally
  • the present invention relates to a process for preparing CO and H 2 from a composite material, the process comprising: a) preparing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining a pyrolysis oil, and optionally adding a further material, obtaining the stream F1 comprising the pyrolysis oil and optionally the further material; and subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally one or more of steam and CO 2 , into a POx reactor being operated at a temperature above 400 °C, and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the one or more of steam and CO 2 , in said reactor, obtaining a raw gas stream S1 comprising CO and H 2 and additionally CO 2 , H 2 O, CH 4 , solid particulates and optional
  • the process of the present invention Using the process of the present invention, it is possible to produce CO and H 2 in large quantities, and the process thus permits, in subsequent steps, the production of new chemical products having a low product carbon footprint (PCF).
  • the process of the present invention also enables a circular economy for important and valuable chemical products, such as amines and reactive diluents for epoxy resins, i.e. 1 ,4-butanediol diglycidyl ether, which can be re-manufac- tured from the CO and H 2 which is provided by the process according to the present invention. This advantage is illustrated in detail hereinunder.
  • providing a feed stream F1 comprising a pyrolysis oil preferably comprises providing a composite material comprising a matrix and a fiber component; suitably comminuting, preferably shredding said composite material, obtaining a comminuted, preferably shredded composite material; and subjecting the obtained shredded composite material to pyrolysis in the pyrolysis reactor, obtaining the pyrolysis oil, which pyrolysis oil is then comprised in F1.
  • the matrix comprised in the composite material used in a) is an organic matrix, more preferably an organic polymeric matrix.
  • the matrix comprised in the composite material comprises at least one of ether groups, ester groups, urethane groups, hydroxy groups, secondary amine groups and tertiary amine groups.
  • the matrix comprised in the composite material is selected from the group consisting of cured epoxy resins, unsaturated polyester resins, polyurethane resins and mixtures of two or more thereof. More preferably, the matrix comprised in the composite material is selected from the group consisting of a cured epoxy resin, an unsaturated polyester resin and a polyurethane resin, more preferably selected from the group consisting of a cured epoxy resin and an unsaturated polyester resin. More preferably, the matrix comprised in the composite material comprises, more preferably is a cured epoxy resin.
  • the cured epoxy resin is obtainable or obtained from one or more selected from the group consisting of bisphenol-A bisglycidyl ether (DGEBA), bisphenol-F bisglycidyl ether, bi- sphenol-S bisglycidyl ether (DGEBS), tetraglycidylmethylene dianiline (TGM-DA), epoxy novo- lacs (the reaction products of epichlorohydrin and phenol resins, novolaks), cycloaliphatic epoxy resins (for instance 3,4-epoxycyclohexylmethyl-3,4-epoxycyclohexanecarboxylate and hexahydrophthalic acid diglycidyl ester) and mixtures of two or more thereof, more preferably from one or more selected from the group consisting of bisphenol-A bisglycidyl ether (DGEBA), oligomeric bisphenol-A bisglycidyl ether, tetraglycidylmethylene dianiline (DGEBA
  • the cured epoxy resin is obtainable or obtained from a mixture of one or more noncured epoxy resins and one or more reactive diluents which are selected from the group consisting of 1 ,4-butanediol diglycidyl ether, 1 ,6-hexanediol diglycidyl ether, glycidyl neodecanoate, glycidyl versatate, 2-ethylhexyl glycidyl ether, C8-C10 alkyl glycidyl ether, C12-C14 alkyl glycidyl ether, p-tert-butyl glycidyl ether, butyl glycidyl ether, nonylphenyl glycidyl ether, p-tert-bu- tylphenyl glycidyl ether, phenyl glycidyl ether, o-cresyl g
  • the cured epoxy resin is obtainable or obtained by a process using a curing agent being an anhydride or an amine.
  • a curing agent being an anhydride or an amine.
  • the terms “curing agent” and “hardener” can be used interchangeably.
  • the amine used as curing agent is selected from the group consisting of epoxy amine adducts, aliphatic amines, aromatic amines, cycloaliphatic amines, and mixtures thereof.
  • the amine is selected from the group consisting of ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, polyetheramine, 4,4'-diaminodiphenylmethane, 4,4’-diaminodicyclohexyl- methane, ), 4,4'-diaminodiphenyl sulfone, 2,4-diaminotoluene, isophoronediamine, methylcyclohexane diamine, 1 ,2-diaminocyclohexane, 1 ,3-diaminocyclohexane, and 1 ,4-diaminocyclo- hexane, polyetheramines, polyamidoamine, mixtures of two or more thereof and adducts comprising epoxy resins reacted with amines thereof.
  • the anhydride is selected from the group consisting of tetrahydrophthalic anhydride, hexahydrophthalic anhydride, methyltetrahydrophthalic anhydride, methylhexahydrophthalic anhydride, benzophenone tetracarboxylic dianhydride, nadic anhydride and mixtures of two or more thereof.
  • the amount of the matrix in the composite material is in the range of from 10 to 80 wt.-%, more preferably of from 20 to 70 wt.-%, more preferably of from 25 to 60 wt.-%, more preferably of from 30 to 50 wt.-%, based on the weight of the composite material. Ranges of from 30 to 40 weight-% or from 35 to 45 weight-% or from 40 to 50 weight-% are conceivable.
  • the fiber component comprised in the composite material is selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers ceramic fibers and mixtures thereof, more preferably the fiber component comprised in the composite material is selected from glass fibers, carbon fibers, aramid fibers, basalt fibers and mixtures thereof, wherein more preferably the fiber component comprised in the composite material is selected from glass fibers, carbon fibers and mixtures of two or more thereof.
  • the composite material comprises one single fiber type.
  • the fiber component comprised in the composite comprises, preferably consists of glass fibers.
  • the amount of the fiber component in the composite material is in the range of from 20 to 89 wt.-%, more preferably of from 25 to 79 wt.-%, more preferably of from 30 to 70 wt.-%, more preferably of from 40 to 60 wt.-%, based on the weight of the composite material. Ranges of from 40 to 50 weight-% or from 45 to 55 weight-% or from 50 to 60 weight-% are conceivable.
  • the amount of both the matrix and the fiber component in the composite material is in the range of from 60 to 100 wt.-%, more preferably of from 70 to 95 wt.-%, based on the weight of the composite material. Ranges of from 70 to 80 weight-% or from 75 to 85 weight-% or from 80 to 90 weight-% or from 85 to 95 weight-% are conceivable.
  • the composite material further comprises one or more of balsa wood, polyvinylchloride foam and polyethylene terephthalate foam.
  • the composite material may further comprise one or more adhesives, such as polyurethane (PU), and one or more coatings.
  • the one or more adhesives represent at most 6 weight-%, more preferably in the range of from 3 to 5 wt.-%, based on the weight of the composite material.
  • the one or more coatings represent at most 3 weight-% based on the weight of the composite material.
  • the sum of the amount of balsa wood, the amount of polyvinylchloride foam and the amount of polyethylene terephthalate foam in the composite material is in the range of from 0.5 to 20 wt.-%, more preferably of from 1 to 15 wt.-%, more preferably of from 1 to 10 wt.-%, more preferably of from 1 to 8 wt.-%, based on the weight of the composite material.
  • the sum of the amount of the matrix, the amount of the fiber component, the amount of balsa wood, the amount of polyvinylchloride foam and the amount of polyethylene terephthalate foam in the composite material is in the range of from 70 to 100 wt.-%, more preferably of from 80 to 95 wt.-%, based on the weight of the composite material.
  • the composite material is selected from the group consisting of one or more parts of an air plane, one or more parts of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, more preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade. Therefore, preferably, the composite material is a wind turbine blade or parts thereof, preferably an end-of- life wind turbine blade or parts thereof.
  • providing F1 comprising the pyrolysis oil according to a) excludes any hydrotreatment step before F1 is subjected to partial oxidation in the POx reactor.
  • Such hydrotreatments are used, for example, for saturating the double bonds of the hydrocarbons in the pyrolysis oil, the removal of heteroatoms, and so on.
  • subjecting the composite material comprising the matrix and the fiber component to pyrolysis comprises: p-1) optionally drying the composite material, more preferably the shredded composite material obtained as defined herein above; p-2) subjecting the optionally dried material obtained in accordance with p-1) to pyrolysis in the pyrolysis reactor at a temperature in the range from 300 to 800 °C and a pressure in the range of from 0.1 to 50 bar(abs), obtaining a crude reactor effluent, comprising a gaseous, liquid and solid phase; p-3) subjecting the crude reactor effluent obtained in accordance with p-2) to a separation step or a sequence of separation steps, thereby separating the fiber component, obtaining the pyrolysis oil.
  • the fiber component can be already separated in step a), thus enabling the realization of high space-time-yields in the subsequent gasification of the pyrolysis oil.
  • the solid phase obtained in p-2) comprises the fiber component. It is conceivable that said fiber component can be reused for preparing other composite materials.
  • the pyrolysis reactor of step p-2) is a batch reactor, a semi-batch reactor, a fixed bed reactor, a shaft reactor, a fluidized bed reactor, a rotary kiln, or a microwave reactor, more preferably a batch reactor, a semi-batch reactor or a fixed bed reactor.
  • the temperature of step p-2) is in the range of from 300 to 700 °C, more preferably in the range of from 300 to 600 °C. Ranges of from 300 to 400 °C or from 350 to 450 °C or from 400 to 500 °C or from 450 to 550 °C or from 500 to 600 °C are conceivable.
  • the pressure in p-2) is in the range of from 0.5 to 10 bar(abs), more preferably in the range of from 0.5 to 2 bar(abs). Ranges of from 0.5 to 1 bar(abs) or from 1 to 1.5 bar(abs) or from 1.5 to 2 bar(abs) are conceivable.
  • the pyrolysis according to a) is performed under an inert atmosphere, more preferably under N 2 atmosphere.
  • the residence time in the pyrolysis reactor is in the range of from 10 min to 3 h, more preferably in the range of from 20 min to 2 h.
  • the residence time it is known in the art that it will depend on the type and/or design of the pyrolysis reactor.
  • the residence time for the pyrolysis is in the range of from 50 min to 2 h.
  • pyrolysis in a can be performed by methods known in the art such as for example disclosed in Wooyoung Yang et aL, “Upcycling of decommissioned wind turbine blades through pyrolysis”, Journal of Cleaner Production 376 (2022) 134292.
  • the pyrolysis is conducted continuously.
  • the pyrolysis oil comprised in F1 provided according to a) exhibits a heating value in the range of from 20,000 to 45,000 J/g, more preferably of from 21 ,000 to 40,000 J/g, more preferably of from 22,000 to 39,000 J/g, more preferably of from 25,000 to 39,0000 J/g, more preferably of from 30,000 to 39,000 J/g, the heating value being measured in accordance with DIN 51900.
  • the pyrolysis oil comprised in F1 provided according to a) exhibits one or more, more preferably two or more, more preferably all of the following parameters: a final boiling point in the range of from 190 to 630 °C, being measured in accordance with ASTM D 86; a viscosity in the range of from 1 to 10 mPa»s, being measured at 40 °C in accordance with DIN 53019; an ash content in the range of from 0 to 17,000 mg/kg, optionally of from 30 to 17,000 mg/kg, being measured in accordance with ISO 6245.
  • the amounts of elementary carbon (C), hydrogen (H), oxygen (O), sulphur (S), and nitrogen (N) in the pyrolysis oil comprised in F1 provided according to a) are as follows: C: 60 to 97 wt.-%, more preferably 70 to 94 wt.-%, based on the weight of the pyrolysis oil;
  • H 1 to 15 wt.-%, more preferably 2 to 10 wt.-%, based on the weight of the pyrolysis oil;
  • O 0 to 25 wt.-% more preferably 2 to 20 wt.-%, based on the weight of the pyrolysis oil; S: 0 to 5 wt.-%, more preferably 0.005 to 4 wt.-%, based on the weight of the pyrolysis oil;
  • N 0 to 5 wt.-%, more preferably 0.005 to 4 wt.-%, based on the weight of the pyrolysis oil.
  • the sum of the amounts of carbon (C), of hydrogen (H), of oxygen (O), of sulphur (S), and of nitrogen (N) in the pyrolysis oil comprised in F1 provided according to a) is in the range of from 70 to 100 wt.-%, more preferably of from 80 to 99.9 wt.-%, more preferably of from 90 to 99.5 wt.-%, more preferably of from 95 to 99.5 wt.-%, based on the weight of the pyrolysis oil.
  • the amount of pyrolysis oil in F1 is in the range of from 1 to 100 wt.-%, more preferably of from 50 to 100 wt.-%, more preferably of from 70 to 100 wt.-%, more preferably of from 90 to 100 wt.-%, based on the weight of F1.
  • F1 may comprise two or more pyrolysis oils, preferably two or more pyrolysis oils from pyrolysis of at least one composite material. If the amount is less than 100 weight-%, it is preferred that providing the stream F1 according to a) comprises adding a further material to the pyrolysis oil, thereby obtaining F1.
  • F1 then further comprises a further material selected from the group consisting of one or more non-gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof, wherein a further material is preferred that exhibits one or more of, more preferably two or more, more preferably three or more, more preferably all of the following parameters: a heating value in the range of from 20,000 to 46,000 J/g, preferably of from 35,400 to 45,300 J/g, more preferably of from 37,000 to 42,000 J/g, being measured in accordance with DIN 51900; a final boiling point in the range of from 190 to 630 °C, being measured in accordance with ASTM D 86; optionally a viscosity in the range of from 1 to 10 mPa»s, being measured at 40 °C in accordance with DIN 53019; an ash content in the range of from 0 to 17000 mg/kg, optionally of from 30 to 17000 mg/kg, being measured in accordance with ISO 62
  • F1 further comprises a further material, wherein the amounts of elementary carbon (C), of hydrogen (H), of oxygen (O), of sulphur (S), and of nitrogen (N) of said further material are as follows:
  • H 1 to 15 wt.-%, more preferably 2 to 10 wt.-%, based on the weight of the material;
  • O 0 to 25 wt.-%, more preferably 1 to 20 wt.-%, based on the weight of the material;
  • S 0 to 5 wt.-%, more preferably 0.005 to 4 wt.-%, based on the weight of the material
  • N 0 to 5 wt.-%, more preferably 0.005 to 4 wt.-%, based on the weight of the material.
  • the sum of the amounts of carbon (C), of hydrogen (H), of oxygen (O), of sulphur (S), and of nitrogen (N) in the further material is in the range of from 70 to 100 wt.-%, more preferably of from 80 to 99.9 wt.-%, more preferably of from 90 to 99.5 wt.-%, more preferably of from 95 to 99.5 wt.-%, based on the weight of the further material.
  • the further material is a non-gaseous organic component such as a liquid organic component
  • the pyrolysis oil and the further material are admixed upstream of the partial oxidation reactor or admixed in the partial oxidation reactor.
  • the further material is a gaseous organic component
  • the pyrolysis oil and the gaseous organic component are passed into the partial oxidation reactor separately via the same means, preferably via the same nozzle.
  • the one or more non-gaseous organic components are selected from the group consisting of bio oils, pyrolysis oils from pyrolysis of biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphaltene fractions, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, industrial waste streams, coal dusts, and mixtures of two or more thereof.
  • the one or more gaseous organic components are selected from the group consisting of natural gas, biogas, cracker fuel gas, and a mixture of two or more thereof.
  • the term “cracker fuel gas” as used herein refers to a byproduct of the petrochemical industry, specifically from the process of "cracking.” “Cracking” is a method used to break down large hydrocarbon molecules into smaller ones, often to produce ethylene, propylene, and other valuable chemicals.
  • the gas produced during this process known as cracker fuel gas, typically contains a mixture of hydrogen, methane, ethane, and other light hydrocarbons.
  • biomass refers to a gaseous renewable energy source produced from raw materials such as agricultural waste, manure, municipal waste, plant material, sewage, green waste, wastewater, and food waste. Biogas is produced by anaerobic digestion with anaerobic organisms or methanogens inside an anaerobic digester, biodigester or a bioreactor.
  • (high) vacuum residue refers to a component which is obtainable or obtained by a process comprising subjecting crude oil, optionally after desalting, the atmospheric distillation, subjecting the atmospheric residue obtained as high-boiling fraction from said atmospheric distillation to vacuum distillation, and obtaining the vacuum residue as high-boiling fraction from said vacuum distillation.
  • composition of the stream S1 it is preferred that from 50 to 100 weight-%, more preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-% of S1 consist of the pyrolysis oil and the further material. Ranges of from 96 to 100 weight-% or from 97 to 100 weight-% or from 98 to 100 weight-%, or from 99 to 100 weight-% are conceivable.
  • the POx reactor used in a) is an entrained flow reactor.
  • the temperature in the POx reactor used in a) is in the range of from 1000 to 2000 °C, more preferably in the range of from 1250 to 1500 °C.
  • the temperature refers to the temperature of the gas atmosphere in the partial oxidation reactor. Ranges of from 1250 to 1350 °C or from 1300 to 1400 °C or from 1350 to 1450 °C or from 1400 to 1500 °C are conceivable.
  • the pressure in the POx reactor used in a) is in the range of from 5 to 200 bar(abs), more preferably of from 10 to 100 bar(abs), more preferably of from 11 to 50 bar(abs). Ranges of from 11 to 30 bar(abs) or from 25 to 35 bar(abs) or from 30 to 40 bar(abs) or from 35 to 45 bar(abs) or from 40 to bar(abs) are conceivable.
  • the weight ratio of O2 to F1 is in the range from 0.4:1 to 1.3:1 , more preferably of from 0.6:1 to 1.2:1 , more preferably of from 0.7 to 1.2:1. Ranges of from 0.7:1 to 0.9:1 or from 0.8:1 to 1.0:1 or from 0.9:1 to 1.1 :1 or from 1.0:1 to 1.2:1 are conceivable.
  • the steam is fed to the reactor in a) and the weight ratio of steam to F1 is equal to or greater than 0.2:1 , more preferably in the range of from 0.3:1 to 2:1 , more preferably of from 0.4:1 to 1.5:1 , more preferably of from 0.4:1 to 1 :1. Ranges of from 0.4:1 to 0.6:1 or from 0.5:1 to 0.7:1 or from 0.6:1 to 0.8:1 or from 0.7:1 to 0.9:1 or from 0.8:1 to 1 :1 are conceivable.
  • CO2 is fed to the reactor in a).
  • the raw gas stream S1 obtained from step a) exhibits a molar ratio of H 2 relative to CO, H 2 :CO, in the range of from 0.5:1 to 1.0:1. Range of from 0.5:1 to 0.7:1 or from 0.6:1 to 0.8:1 or from 0.7:1 to 0.9:1 or from 0.8:1 to 1.0:1 are conceivable.
  • the first purification stage according to b) comprising: b-1 ) subjecting the stream S1 obtained according to a) to a washing step in a washing unit, more preferably the washing unit being a column having a spray nozzle or an atomizer located at the top of the column, obtaining a stream S11 depleted in particulate solid compared to S1 and comprising CO, H 2 , CO 2 , H 2 O, CH 4 , and optionally H 2 S; b-2) subjecting the stream S11 obtained according to b-1 ) to a drying step in a drying unit, obtaining a stream S12 depleted in H2O compared to S11 and S1 ; b-3) subjecting the stream S12 obtained according to b-2) to an acid gas removal step in a CO2/H2S adsorption unit, more preferably the CO2/H2S adsorption unit is an absorption column, obtaining the stream S2.
  • b-1 comprising contacting S1 with water in the
  • the drying unit used in b-2) is a water separation unit.
  • b-2) comprises cooling the stream S11 obtained according to b-1 ), obtaining S12, a gaseous stream, separated from water condensate.
  • the drying step can be performed as disclosed in WO2023/161302A1.
  • b-3) comprises subjecting the stream S12 obtained according to b-2) to an acid gas removal step in a CO2/H2S adsorption unit, more preferably the CO2/H2S adsorption unit is an absorption column, obtaining the stream S2 and a stream S C o2 comprising CO2.
  • S C o2 is recycled in the process of the present invention.
  • Sco2 is recycled in c-2) as at least a portion of the source of CO2 in c-2).
  • c) comprises c-1) passing and contacting water with the purified gas stream S2 obtained in accordance with b) into a reaction unit RU(1) and subjecting to a water gas shift reaction in RU(1), obtaining a stream S2’(1) depleted in CO compared to S2 and comprising CO, H 2 , CH4 and CO2; or c-2) passing and contacting CO2, optionally Sco2, with the purified gas stream S2 obtained in accordance with b) into a reaction unit RU(2) for a reverse water gas shift reaction, obtaining a stream S2’(2) enriched in CO compared to S2 and comprising CO, H2 and CH4; or c-3) adding H 2 to the purified gas stream S2 obtained in accordance with b), obtaining a stream S2’(3) enriched in H 2 compared to S2 and comprising CO, H2 and CH4.
  • the water gas shift reaction is preferably performed according to known processes in the art, such as for example those defined in Wei-Hsin Chen, et aL, “Water gas shift reaction for hydrogen production and carbon dioxide capture”, Applied energy 258 (2020) 114078, https://doi.Org/10.1016/j.apenergy.2019.114078.
  • the reverse water gas shift reaction is preferably performed according to known processes in the art such as for example those defined in E.Rezaei, S. Dzuryk “Techno-economic comparison of reverse water gas shift reaction to steam and dry methane reforming reactions for syngas production", Chemical Engineering Research and Design, Vol 144 (2019), S. 354-369, EP2175986, CN 103183346 and US8946308.
  • the process further comprises passing S2’(1) in an acid gas removal unit, obtaining a stream S2’(11) depleted in CO 2 compared to S2’(1) and comprising CO, H 2 and CH 4 .
  • At least a portion of the added H 2 is renewably sourced H 2 .
  • d) comprises subjecting the purified gas stream S2 obtained in accordance with b), or the modified gas stream S2’ obtained in accordance with c), to a second purification stage, comprising introducing S2 or S2’ in a cold box, obtaining CO in a gas stream S3, H 2 in a gas stream S4 and CH 4 in a gas stream S5.
  • a cold box can separate CO, H 2 and CH 4 (cryogenic separation) such that it is possible to obtain three different streams.
  • cryogenic separation as in d) can be performed by method known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, Carbon Monoxide, Chapter 4.3.2, p.685-686.
  • the process further comprises e) subjecting at least a portion of S3 comprising CO obtained in accordance with d) and/or at least a portion of S4 comprising H 2 obtained in accordance with d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products.
  • the present invention specifically relates to a highly advantageous pathway to close the recycle loop of a composite material eco system by providing the steps necessary to manufacture new starting material from end-of-life composite materials, which starting materials are then suitably used to produce new materials including, but not restricted to, new composite materials.
  • the present invention also relates to a process for preparing one or more chemical products, the process comprising: a) preparing or providing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining a pyrolysis oil, and optionally adding a further marerial, obtaining the stream F1 comprising the pyrolysis oil and optionally the further material; and subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally one or more of steam and CO 2 , into a POx reactor being operated at a temperature above 400 °C, and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the one or more of steam and CO 2 , in said reactor, obtaining a raw gas stream S1 comprising CO and H2 and additionally CO2, H2O, CH4, solid particulates and optionally H 2 S
  • CO and/or H 2 used in e is blended or used interchangeably with CO and/or H2 from another source.
  • e) further comprises additionally using a source of CO which is not S3 and/or using a source of H2 which is not S4.
  • e) comprises: e-1 ) bringing in contact CO comprised in S3 obtained in accordance with d) with methanol and subjecting CO and methanol to a chemical conversion, obtaining a stream S7 comprising a first chemical product being methyl formate; e-2) optionally bringing in contact at least a portion of S7 obtained according to e-1) with ammonia and subjecting said portion of S7 and ammonia to a chemical conversion, obtaining a stream S8 comprising methanol and a second chemical product being formamide; e-3) optionally separating formamide from methanol comprised in S8 obtained according to e- 2) and optionally recycling methanol in e-1), obtaining a stream S81 depleted in methanol compared to S8 and comprising formamide; e-4) optionally subjecting at least a portion of S8 obtained according to e-2) or at least a portion of S81 obtained according to e-3) to a thermal decomposition and subsequent water removal, obtaining
  • e) further comprises: e-5) bringing in contact at least a portion of S9 obtained according to e-4) with isophorone and subjecting to a chemical conversion, being a Michael addition reaction, obtaining a stream S10 comprising isophorone nitrile; e-6) optionally subjecting at least a portion of S10 obtained according to e-5) to hydrogenation, preferably using H2 obtained in accordance with d), in the presence of ammonia, obtaining a stream P comprising a chemical product being isophorone diamine.
  • e) comprises subjecting an alcohol, a ketone, or an aldehyde to a chemical conversion with ammonia, a primary or secondary amine in the presence of H 2 obtained in accordance with d), and a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being an amine.
  • e) comprises subjecting an organic nitrile to a hydrogenation reaction in the presence of H 2 obtained in accordance with step d), and a heterogenous catalyst, obtaining a chemical product being an amine.
  • the organic nitrile is obtained by a process comprising subjecting an alkene to a chemical conversion with hydrogen cyanide obtained in accordance with e-4) as defined herein.
  • the alkene referred to above is neither a butadiene nor a pentenenitrile.
  • the chemical conversion of a butadiene and/or a pentenenitrile with hydrogen cyanide obtained in accordance with e-4) is explicitly excluded from the subject-matter and scope of this invention.
  • e) comprises hydrogenating an organic nitro compound with H 2 obtained in accordance with d), obtaining a chemical product being an amine.
  • e) comprises subjecting CO comprised in S3 obtained in accordance with d) to a chemical conversion with gaseous chlorine, obtaining a chemical product being phosgene; and optionally subjecting at least a portion of the obtained phosgene to a chemical conversion with an amine, obtaining a further chemical product being an isocyanate. More preferably, said amine is obtained as defined herein.
  • e) comprises subjecting a mixture of CO and H 2 , both obtained in accordance with d), to a chemical conversion in the presence of a heterogeneous catalyst, obtaining a chemical product being methanol. More preferably, e) further comprises subjecting at least a portion of the obtained methanol to a partial oxidation reaction, obtaining a chemical product being formaldehyde. Preferably, e) further comprises subjecting at least a portion of the obtained formaldehyde to a chemical conversion, being a Reppe reaction, with acetylene, obtaining a chemical product being 1 ,4-butyndiole; optionally subjecting at least a portion of the obtained
  • e) further comprises subjecting at least a portion, or a portion, of the obtained methanol to a chemical conversion in the presence of a zeolite catalyst, obtaining a mixture comprising ethylene and propylene; subjecting the obtained mixture to one or more separation steps, obtaining two separated chemical products: a first chemical product being ethylene and a second chemical product being propylene.
  • e) comprises subjecting a mixture of CO and H2, CO and/or H2, preferably CO and H 2 , being obtained in accordance with d), to a Fischer-Tropsch synthesis, obtaining a mixture of hydrocarbons; and subjecting the obtained mixture of hydrocarbons to one or more separation steps, obtaining chemical products being one or more alkenes, more preferably one or more of ethylene and propylene.
  • e) comprises subjecting a polyether alcohol to a chemical conversion with ammonia in the presence of H2 obtained in accordance with d), and a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being a polyether amine.
  • the polyether alcohol is selected from the group consisting of polypropylene glycols, polyethylene glycols and polypropylene ethylene glycol copolymers, such polyether alcohol being obtained by a process comprising subjecting, where required, ethylene and/or propylene, any of which being obtained by the process disclosed herein to a partial oxidation, obtaining ethylene oxide and/or propylene oxide; subjecting the obtained ethylene oxide and/or propylene oxide to a polymerization reaction, obtaining the respective polyether alcohol.
  • the polyether alcohol is a polypropylene glycol having a number average molecular weight in the range from 200 to 3000 g/mol, more preferably in the range from 210 to 2100 g/mol, more preferably in the range from 210 to 500 g/mol.
  • the different chemical products obtained according to e) can be prepared according to processes known in the art such as for example as described in K. Weissermel, H.-J. Arpe, Industrial Organic Chemistry, Chapter 2, 4 th Ed., Wiley VCH 2003.
  • the polyetheramine obtained according to e) can be prepared as disclosed in WO2016/091643A1 .
  • e) comprises: providing an epoxy resin and an amine; providing a fiber component selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers, ceramic fibers, mixtures thereof, more preferably the fiber component is selected from glass fibers, carbon fibers, aramid fibers, basalt fibers, mixtures thereof, more preferably the fiber component is selected from glass fibers, carbon fibers, and mixtures thereof; curing the epoxy resin with the amine in the presence of the fiber component, obtaining a chemical product being a composite material; wherein at least one of the following two conditions applies: the epoxy resin is 1 ,4-butanediol-diglycidylether obtained in accordance with the process disclosed herein; the amine is an amine obtained in accordance with the process disclosed herein.
  • the present invention further relates to a recycling process for the provision of a pyrolysis oil, comprising the steps of: a) providing a material comprising a chemical product manufactured according to the process according to the present invention;
  • the present invention further relates to a process for recycling a composite material CM(1 ), the process comprising: a’) providing or preparing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material CM(1) comprising a matrix and a fiber component, to pyrolysis in a pyrolysis reactor, obtaining the stream F1 comprising the pyrolysis oil; subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally steam, into a POx reactor being operated at a temperature above 400 °C and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the steam, into said reactor, obtaining a raw gas stream S1 comprising in addition to CO and H 2 , CO 2 , H 2 O, CH4, solid particulates and optionally H 2 S; b’) subjecting S1 obtained in accordance with a’) to a first purification stage, obtaining a purified
  • the present invention yet further relates to a process for recycling a composite material CM(1), the process comprising: a’) providing or preparing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining a pyrolysis oil, and optionally adding a further material, obtaining the stream F1 comprising the pyrolysis oil and optionally the further material; and subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally one or more of steam and CO 2 , into a POx reactor being operated at a temperature above 400 °C, and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O2, and optionally the one or more of steam and CO2, in said reactor, obtaining a raw gas stream S1 comprising CO and H2 and additionally CO2, H2O, CH4, solid particulates and optionally H 2 S; b
  • the composite material CM(1) is selected from the group consisting of one or more parts of an air plane, one or more parts of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, more preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade. Therefore, preferably, CM(1) is wind turbine blades.
  • the composite material CM(2) is wind turbine blades or a composite material other than wind turbine blades, such as selected from the group consisting of one or more parts of an air plane, one or more parts of a car, one or more parts of a ship, and a mixture of two or more thereof.
  • steps a’), b’) c’), d’) and e’) are preferably further described as described in the foregoing regarding the steps a), b), c), d) and e), respectively.
  • According to another aspect of the present invention relates to a process, preferably a process as defined hereinabove, comprising the step of converting a chemical material obtainable or obtained by said process as defined hereinabove, to obtain a product Q.
  • the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acry- late hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic
  • the content of the chemical material in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and/or the content of the chemical material in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and/or segregation and/or mass balance and/or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.
  • ISCC International Sustainability and Carbon Certification
  • Reference RF1 The publication Prior Art Disclosure; Issue 684; paragraphs [1000] to [8005]; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety.
  • the product Q referred to in the preceding paragraph is a product as described in Reference RF1 ; paragraphs [1000] to [8005],
  • the process described herein is further a process for the production of a product, preferably product Q.
  • the converting step to obtain the product Q preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art.
  • the converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and/or steam cracking; and/or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and/or subjecting to ion exchanger; and/or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and/or compounding; and/or forming, preferably foaming, extruding and/or molding; and/or finishing, preferably coating and/or smoothing.
  • building block comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and/or higher molecular weight than the building block on which the secondary product is based.
  • the building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic com-pounds.
  • the alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.
  • the term “monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization.
  • the monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates.
  • (Meth)acry- lates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms.
  • (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable.
  • the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.
  • the building block can further be an intermediate compound.
  • intermediate compound as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity.
  • the intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide.
  • the polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and/or diphenylmethane diisocyanate (MDI).
  • polymer A comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs [2001] to [2007] of Reference RF1 .
  • polymer composition A comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and/or flame retardant, and is defined in more detail in paragraph [2008] of Reference RF1.
  • additive(s) e.g. reinforcement, colorant, modifier and/or flame retardant
  • polymer product A comprises any product comprising the polymer A and/or polymer composition A as described above and is defined in more detail in paragraphs [2009] and [2010] of Reference RF1 .
  • the step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is/are described in more detail in paragraph [2011] of Reference RF1 .
  • the term “industrial use polymer”, as used in the context of the product Q herein, comprises rhe-ology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, poly- ether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs [3035] to [3044] of Reference RF1.
  • the term “industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs [3008] to [3034] of Reference RF1.
  • the term “industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs [3001] to [3005] of Reference RF1.
  • the term “industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs [3006] to [3007] of Reference RF1.
  • the term “industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs [3045] to [3055] of Reference RF1.
  • the term “industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs [3056] to [3058] of Reference RF1 .
  • composition and/or formulation thereof with reference to the industrial use polymers, industrial use surfactants, descaling compounds and/or industrial use biocides refers to industrial use compositions and/or institutional use products and/or fabric and home care products and/or personal care products defined in more detail in paragraph [3059] of Reference RF1.
  • the converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3060] of Reference RF1 .
  • the converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3061] of Reference RF1.
  • agrochemical composition typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary.
  • agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph [4001],
  • the agrochemical composition may take the form of any customary formulation.
  • the agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grube- mann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005.
  • the converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes.
  • active pharmaceutical ingredients and/or intermediates thereof comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient.
  • pharmaceutical excipients as used in the context of the product Q herein, comprises com- pounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph [5001] of Reference RF1.
  • the converting step(s) to obtain the active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • animal feed additives human food additives, dietary supplements, as used in the con-text of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propi
  • aqueous polymer dispersion comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section [6001] entitled “aqueous polymer dispersion” of Reference RF1.
  • the dispersed polymers may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s).
  • emulsion polymer comprises polymer(s) made by free-radical emulsion polymerization.
  • Aqueous polyurethane dispersions are defined in more detail in the section [6002] entitled “Polyurethane dispersions” of Reference RF1.
  • UV-curable polyurethane(s) is/are defined in more detail in the section [6017] of Reference RF1.
  • Polyurethane - poly(meth)acrylate hybrid polymer(s) is/are defined in more detail in the section [6016] of Reference RF1 .
  • polymeric dispersant comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph [6020] entitled “Polymeric dispersant” of Reference RF1 .
  • the converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is/are defined in more detail in the section [6014] entitled “Process for the preparation of aqueous poly-urethane dispersions” and section [6017)] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1 .
  • Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section [6010] entitled “Polyisocyanates” of Reference RF1.
  • Hyperbranched polyester polyol(s) and its/their uses are defined in more detail in section [6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating com-positions” of Reference RF1.
  • the converting step(s) to obtain the hyperbranched polyester polyols is/are defined in more detail in the section [6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1 .
  • Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section [6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.
  • Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section [6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1.
  • 100% curable coating composition(s) is/are defined in more detail in section [6019] of Reference RF1.
  • Polymeric dispersant(s) for inorganic binder compositions is/are defined in more detail in section [6020] of Reference RF1.
  • the inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section [6021] of Reference RF1.
  • the converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section [6020] of Reference RF1.
  • the term “inorganic binder composition” comprising the polymeric dispersants” comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section [6021] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”.
  • Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section [6021] of Reference RF1 .
  • cosmetic surfactant as used in the context of the product Q herein, comprises nonionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph [7002] of Reference RF1.
  • emollient as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and/or lubricating the skin and is defined in more detail in paragraph [7003] of Reference RF1.
  • wax as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph [7004] of Reference RF1 .
  • cosmetic polymer as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph [7005] of Reference RF1 .
  • UV filter as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph [7006] of Reference RF1.
  • further cosmetic ingredient as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation.
  • Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients.
  • composition and/or formulation thereof with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and/or further cosmetic ingredient refers to personal care and/or cosmetic compositions or formulations defined in more detail in paragraph [7007] of Reference RF1.
  • the converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is/are defined in more detail in paragraph [7008] of Reference RF1 .
  • the present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated.
  • every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2 and 3".
  • the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.
  • providing the feed stream F1 comprising a pyrolysis oil according to a) comprises providing a composite material comprising a matrix and a fiber component; suitably comminuting, preferably shredding said composite material, obtaining a comminuted, preferably shredded composite material; and subjecting the obtained shredded composite material to pyrolysis in the pyrolysis reactor, obtaining the stream F1 comprising the pyrolysis oil.
  • the cured epoxy resin is obtainable or obtained from one or more selected from the group consisting of bisphenol-A bis- glycidyl ether (DGEBA), bisphenol-F bisglycidyl ether, bisphenol-S bisglycidyl ether (DGEBS), tetraglycidylmethylene dianiline (TGM-DA), epoxy novolacs (the reaction products of epichlorohydrin and phenol resins, novolaks), cycloaliphatic epoxy resins (for instance 3,4-epoxycyclohexylmethyl-3,4-epoxycyclohexanecarboxylate and hexahydrophthalic acid diglycidyl ester) and mixtures of two or more thereof; wherein the resin is preferably obtainable or obtained from a mixture of one or more noncured epoxy resins and one or more reactive diluents, which reactive diluents are selected from the group consisting of 1 ,4
  • a curing agent being an anhydride or an amine.
  • the amine is selected from the group consisting of epoxy amine adducts, aliphatic amines, aromatic amines, cycloaliphatic amines, and mixtures of two or more thereof.
  • amine is selected from the group consisting of ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, polyetheramine, 4,4'-diaminodiphenylmethane, 4,4’-diaminodicyclohexylmethane, ), 4,4'- diaminodiphenyl sulfone, 2,4-diaminotoluene, isophoronediamine, methylcyclohexane diamine, 1 ,2-diaminocyclohexane, 1 ,3-diaminocyclohexane, and 1 ,4-diaminocyclohexane, polyetheramines, polyamidoamine, mixtures of two or more thereof and adducts comprising epoxy resins reacted with amines thereof.
  • anhydride is selected from the group consisting of tetrahydrophthalic anhydride, hexahydrophthalic anhydride, methyltetrahydrophthalic anhydride, methylhexahydrophthalic anhydride, benzophenone tetracarboxylic dianhydride, nadic anhydride and mixtures of two or more thereof.
  • any one of embodiments 2 to 11 wherein the amount of the matrix in the composite material is in the range of from 10 to 80 wt.-%, preferably of from 20 to 70 wt.- %, more preferably of from 25 to 60 wt.-%, more preferably of from 30 to 50 wt.-%, based on the weight of the composite material.
  • any one of embodiments 1 to 26, wherein subjecting the composite material, as defined in any one of embodiments 2 to 21 , comprising the matrix and the fiber component to pyrolysis comprises: p-1) optionally drying the composite material, preferably the shredded composite material obtained according to embodiment 3; p-2) subjecting the optionally dried material obtained in accordance with p-1) to pyrolysis in the pyrolysis reactor at a temperature in the range from 300 to 800 °C and a pressure in the range of from 0.1 to 50 bar(abs), obtaining a crude reactor effluent, comprising a gaseous, liquid and solid phase; p-3) subjecting the crude reactor effluent obtained in accordance with p-2) to a separation step or a sequence of separation steps, thereby separating the fiber component, obtaining the pyrolysis oil.
  • step p-2 is a batch reactor, a semi-batch reactor, a fixed bed reactor, a shaft reactor, a fluidized bed reactor, a rotary kiln, or a microwave reactor, preferably is a batch reactor, a semi-batch reactor or a fixed bed reactor.
  • the temperature of step p-2) is in the range of from 300 to 700 °C, preferably in the range of from 300 to 600 °C.
  • H 1 to 15 wt.-%, preferably 2 to 10 wt.-%, based on the weight of the pyrolysis oil;
  • N 0 to 5 wt.-%, preferably 0.005 to 4 wt.-%, based on the weight of the pyrolysis oil.
  • F1 further comprises a further material that exhibits one or more of the following parameters: a heating value in the range of from 20,000 to 46,000 J/g, preferably of from 35,400 to 45,300 J/g, more preferably of from 37,000 to 42,000 J/g (measured in accordance with DIN 51900); a final boiling point in the range of from 190 to 630 °C (measured in accordance with ASTM D 86); optionally a viscosity in the range of from 1 to 10 mPa s (measured at 40 °C in accordance with DIN 53019); an ash content in the range of from 0 to 17000 mg/kg, optionally of from 30 to 17000 mg/kg (measured in accordance with ISO 6245).
  • a heating value in the range of from 20,000 to 46,000 J/g, preferably of from 35,400 to 45,300 J/g, more preferably of from 37,000 to 42,000 J/g (measured in accordance with DIN 51900); a final boiling point in the range
  • F1 further comprises a further material, wherein the amount of elementary carbon (C), of hydrogen (H), of oxygen (O), of sulphur (S), and of nitrogen (N) of said further material is as follows:
  • C 60 to 99 wt.-%, preferably 70 to 96 wt.-%, based on the weight of the material; H: 1 to 15 wt.-%, preferably 2 to 10 wt.-%, based on the weight of the material;
  • O 0 to 25 wt.-%, preferably 1 to 20 wt.-%, based on the weight of the material; S: 0 to 5 wt.-%, preferably 0.005 to 4 wt.-%, based on the weight of the material;
  • N 0 to 5 wt.-%, preferably 0.005 to 4 wt.-%, based on the weight of the material.
  • e) comprises: e-1 ) bringing in contact CO comprised in S3 obtained in accordance with d) with methanol and subjecting CO and methanol to a chemical conversion, obtaining a stream S7 comprising a first chemical product being methyl formate; e-2) optionally bringing in contact at least a portion of S7 obtained according to e-1) with ammonia and subjecting said portion of S7 and ammonia to a chemical conversion, obtaining a stream S8 comprising methanol and a second chemical product being formamide; e-3) optionally separating formamide from methanol comprised in S8 obtained according to e-2) and optionally recycling methanol in e-1), obtaining a stream S81 depleted in methanol compared to S8 and comprising formamide; e-4) optionally subjecting at least a portion of S8 obtained according to e-2) or at least a portion of S81 obtained according to
  • e) further comprises: e-5) bringing in contact at least a portion of S9 obtained according to e-4) with isophorone and subjecting to a chemical conversion, being a Michael addition reaction, obtaining a stream S10 comprising isophorone nitrile; e-6) optionally subjecting at least a portion of S10 obtained according to e-5) to hydrogenation, preferably using H2 obtained in accordance with d), in the presence of ammonia, obtaining a stream P comprising a chemical product being isophorone diamine. 47.
  • e) comprises subjecting an alcohol, a ketone, or an aldehyde to a chemical conversion with ammonia, a primary or secondary amine in the presence of H 2 obtained in accordance with d), and a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being an amine.
  • step e) comprises subjecting CO obtained in accordance with d) to a chemical conversion with gaseous chlorine, obtaining a chemical product being phosgene; and optionally subjecting at least a portion of the obtained phosgene to a chemical conversion with an amine, obtaining a further chemical product being an isocyanate.
  • polyether alcohol is selected from the group consisting of polypropylene glycols, polyethylene glycols and polypropylene ethylene glycol copolymers, such polyether alcohol being obtained by a process comprising subjecting, where required, ethylene and/or propylene, any of which being obtained in accordance with embodiment 56 or 57 to a partial oxidation, obtaining ethylene oxide and/or propylene oxide; and subjecting the obtained ethylene oxide and/or propylene oxide to a polymerization reaction, obtaining the respective polyether alcohol.
  • polyether alcohol is a polypropylene glycol having a number average molecular weight in the range from 200 to 3000 g/mol, preferably in the range from 210 to 2100 g/mol, more preferably in the range from 210 to 500 g/mol.
  • e) comprises: providing an epoxy resin and an amine; providing a fiber component selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers, ceramic fibers, mixtures thereof, preferably the fiber component is selected from glass fibers, carbon fibers, aramid fibers, basalt fibers, mixtures thereof, more preferably the fiber component is selected from glass fibers, carbon fibers, and mixtures thereof; curing the epoxy resin with the amine in the presence of the fiber component, obtaining a chemical product being a composite material; wherein at least one of the following two conditions applies: the epoxy resin is 1 ,4-butanediol-diglycidylether obtained in accordance with embodiment 55, the amine is an amine obtained in accordance with any one of embodiments 46 to 50 and 58 to 60.
  • PA polyamide
  • TPU thermoplastic polyure
  • a process for recycling a composite material CM(1) comprising: a’) providing or preparing a feed stream F1 comprising a pyrolysis oil, comprising subjecting the composite material comprising a matrix and a fiber component to pyrolysis in a pyrolysis reactor, obtaining a pyrolysis oil, and optionally adding a further material, obtaining the stream F1 comprising the pyrolysis oil and optionally the further material; and subjecting F1 to partial oxidation POx, comprising introducing F1 , O 2 , and optionally one or more of steam and CO 2 , into a POx reactor being operated at a temperature above 400 °C, and at a pressure of 1 bar(abs) or more, bringing in contact F1 with O 2 , and optionally the one or more of steam and CO 2 , in said reactor, obtaining a raw gas stream S1 comprising CO and H2 and additionally CO2, H2O, CH4, solid particulates and optionally H2S; b’) subjecting S1
  • the composite material CM(1) is selected from the group consisting of one or more parts of an air plane, one or more parts of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material CM(1 ) comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade; and wherein the composite material CM (2) is preferably selected from the group consisting of one or more parts of a wind turbine blade, one or more parts of an air plane, one or more parts of a car, one or more parts of a ship, and a mixture of two or more thereof.
  • a process preferably according to any one of embodiments 1 to 68, comprising the step of converting a chemical material obtainable or obtained by the process according to any one of embodiments 1 to 68 to obtain a product Q.
  • the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient,
  • X is a chemical element and A, B and C are con- crete elements such as Li, Na, and K, or X is a temperature and A, B and C are concrete temperatures such as 10 °C, 20 °C, and 30 °C.
  • X is one or more of A and B” disclosing that X is either A, or B, or A and B, or to more specific realizations of said feature, e.g. “X is one or more of A, B, C and D”, disclosing that X is either A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D, or A and B and C and D, or A and B and C and D, or A and B and C and D, or A and B and C and D.
  • Wind turbine blades were shredded to obtain pieces which were then introduced in a pyrolysis batch reactor.
  • the parts of the blades which were used were parts of the roots of end-of-life wind turbine blades.
  • the pyrolysis of the pieces of the wind blades was performed at a temperature of 300 to 600 °C and a pressure of 1 bar(abs) under inert atmosphere (N 2 ) and at a residence time of 90 min.
  • N 2 inert atmosphere
  • a gas stream was removed and condensed for obtaining a stream F1 comprising a pyrolysis oil.
  • the examples are based on simulations performed via the flow sheet simulation platform Aspen Plus V14.0.
  • the first example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1 ) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream (1) comprises 80.4 wt.-% carbon, 7.7 wt.-% hydrogen, 11.8 wt.-% oxygen and 0.1 wt.-% nitrogen. Additionally, gasification agents are injected into the gasifier, enabling the gasification reaction at a temperature of 1350 °C.
  • the gasification agents are oxygen with a mass flow of 10.77 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 4 t/h at 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas stream (S1) comprising CO, H 2 O, CO 2 , H 2 , CF , N 2 , NH3, ash and tars was washed with water (4) and dried (at 100 to 150 °C) in order to reduce the amount of water, ash and tars.
  • the synthesis gas (3) was subjected to acid gas removal, by amine scrubbing, to separate acids like CO 2 (7) with a mass flow of 7.94 t/h from the raw synthesis gas.
  • the obtained (clean) synthesis gas stream (S2) comprises 47.6 vol.-% H 2 , 52.3 vol.-% CO, 0.1 vol.-% H 2 O at a total mass flow of 15.41 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H 2 in a gas stream S4 and CH4 in a gas stream S5.
  • the second example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1 ) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream (F1 ) comprises 88.0 wt.-% carbon, 9.0 wt.-% hydrogen, 3.0 wt.-% oxygen and 0.0 wt.-% nitrogen.
  • gasification agents are injected into the gasifier, enabling the gasification reaction at a temperature of 1350 °C.
  • the gasification agents are oxygen with a mass flow of 12.24 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 4 t/h and at 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas stream (S1) comprising CO, H 2 O, CO 2 , H 2 , CH 4 , N 2 , NH3, ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars.
  • the clean synthesis gas stream (S2) comprises 42.7 vol.-% H 2 , 57.1 vol.-% CO, 0.2 vol.-% H 2 O at a total mass flow of 20.31 t/h.
  • the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H 2 in a gas stream S4 and CH 4 in a gas stream S5.
  • the third example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1 ) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream (F1) comprises 65.0 wt.-% carbon, 6.0 wt.-% hydrogen, 29.0 wt.-% oxygen and 0.0 wt.-% nitrogen.
  • gasification agents are injected into the gasifier, enabling the gasification reaction at a temperature of 1350 °C.
  • the gasification agents are oxygen with a mass flow of 8.16 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 4 t/h at 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas stream (S1) comprising CO, H 2 O, CO 2 , H 2 , CH 4 , N 2 , NH3, ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars. After the washing and drying steps, the acid gas removal, enabled by amine scrubbing, was used to separate acids like CO 2 with a mass flow of 5.21 t/h from the synthesis gas.
  • the clean synthesis gas stream S2 comprises 39.6 vol.-% H 2 , 60.3 vol.-% CO, 0.1 vol.-% H 2 O at a total mass flow of 13.1 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H 2 in a gas stream S4 and CH 4 in a gas stream S5.
  • the fourth example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream F1 comprises 80.4 wt.-% carbon, 7.7 wt.-% hydrogen, 11.8 wt.-% oxygen and 0.1 wt.-% nitrogen.
  • gasification agents are injected into the gasifier, enabling the gasification reaction at a temperature of 1450 °C.
  • the gasification agents are oxygen with a mass flow of 11 .13 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 4 t/h and 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas stream S1 comprising CO, H2O, CO2, H2, CH4, N2, NH3, ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars. After the washing and drying steps, the acid gas removal, enabled by amine scrubbing, was used to separate acids like CO2 with a mass flow of 3.93 t/h from the synthesis gas.
  • the clean synthesis gas stream S2 comprises 40.2 vol.-% H 2 , 59.6 vol.-% CO, 0.2 vol.-% H 2 O at a total mass flow of 17.84 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H 2 in a gas stream S4 and CH 4 in a gas stream S5.
  • the fifth example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1 ) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream (F1) comprises 80.4 wt.-% carbon, 7.7 wt.-% hydrogen, 11.8 wt.-% oxygen and 0.1 wt.-% nitrogen. Additionally, gasification agents were injected into the gasifier, enabling the gasification reaction at a temperature of 1200 °C.
  • the gasification agents are oxygen with a mass flow of 10.22 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 4 t/h and 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas S1 comprising CO, H2O, CO2, H2, CH 4 , N2, NH3, ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars. After the washing and drying steps, the acid gas removal, enabled by amine scrubbing, was used to separate acids like CO 2 with a mass flow of 3.79 t/h from the synthesis gas.
  • the clean synthesis gas stream S2 comprises 42.7 vol.-% H 2 , 56.9 vol.-% CO, 0.4 vol.-% H 2 O at a total mass flow of 17.99 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H2 in a gas stream S4 and CH 4 in a gas stream S5.
  • the sixth example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream (F1) comprises 80.4 wt.-% carbon, 7.7 wt.-% hydrogen, 11.8 wt.-% oxygen and 0.1 wt.-% nitrogen.
  • gasification agents were injected into the gasifier, enabling the gasification reaction at a temperature of 1350 °C.
  • the gasification agents are oxygen with a mass flow of 11 .64 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 10.4 t/h and 400 °C and 47 bar(abs).
  • the resulting raw synthesis gas S1 comprising CO, H2O, CO2, H2, CH4, N2, NH3, ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars. After the washing and drying steps, the acid gas removal, enabled by amine scrubbing, was used to separate acids like CO 2 with a mass flow of 7.94 t/h from the synthesis gas.
  • the clean synthesis gas stream S2 comprises 47.6 voL-% H 2 , 52.3 voL-% CO, 0.1 voL-% H2O at a total mass flow of 15.41 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H2 in a gas stream S4 and CH4 in a gas stream S5.
  • the seventh example comprises a partial oxidation of pyrolysis oil, originated by wind blades (composite material), in an entrained flow reactor (gasifier).
  • the reactor was fed with a feed stream (F1 ) (comprising a pyrolysis oil, originated from the pyrolysis of wind blades as described in Ref. Ex. 1 herein above) at a mass flow of 10.4 t/h at 47 bar(abs) and 100 °C.
  • the feed stream F1 comprises 80.4 wt.-% carbon, 7.7 wt.-% hydrogen, 11.8 wt.-% oxygen and 0.1 wt.-% nitrogen.
  • gasification agents were injected into the gasifier, enabling the gasification reaction at a temperature of 1350 °C.
  • the gasification agents are oxygen with a mass flow of 11 .64 t/h at 47 bar(abs) and 25 °C, as well as steam with a mass flow of 0 t/h.
  • the resulting raw synthesis gas S1 comprising CO, H 2 O, CO 2 , H 2 , CH 4 , N 2 , NH 3 , ash and tars was washed with water and dried in order to reduce the amount of water, ash and tars. After the washing and drying steps, the acid gas removal, enabled by amine scrubbing, was used to separate acids like CO2 with a mass flow of 0.39 t/h from the synthesis gas.
  • the clean synthesis gas stream S2 comprises 35.1 voL-% H2, 64.3 voL-% CO, 0.6 voL-% H2O at a total mass flow of 19.96 t/h. Subsequently, the stream S2 was subjected to a purification stage, using a cold box, for obtaining CO in a gas stream S3, H2 in a gas stream S4 and CH4 in a gas stream S5.

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Abstract

La présente invention concerne un procédé de préparation de monoxyde de carbone (CO) et d'hydrogène moléculaire (H2) à partir d'une huile de pyrolyse, en particulier à partir d'un matériau composite tel que des pales d'éolienne. La présente invention concerne en outre des procédés de recyclage.
PCT/EP2024/087425 2023-12-20 2024-12-19 Procédé de préparation de monoxyde de carbone (co) et d'hydrogène moléculaire (h2) Pending WO2025132804A1 (fr)

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