EP4347677A1 - Pyrolyse d'une matière contenant un composé de polyuréthane afin de récupérer des matières premières - Google Patents

Pyrolyse d'une matière contenant un composé de polyuréthane afin de récupérer des matières premières

Info

Publication number
EP4347677A1
EP4347677A1 EP22731580.1A EP22731580A EP4347677A1 EP 4347677 A1 EP4347677 A1 EP 4347677A1 EP 22731580 A EP22731580 A EP 22731580A EP 4347677 A1 EP4347677 A1 EP 4347677A1
Authority
EP
European Patent Office
Prior art keywords
pyrolysis
reactor
pyrolysate
weight
compound
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP22731580.1A
Other languages
German (de)
English (en)
Inventor
Stefanie Eiden
Rainer Bellinghausen
Aurel Wolf
Christian Hahn
Tim Loddenkemper
Carola JENDRZOK
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Covestro Deutschland AG
Original Assignee
Covestro Deutschland AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Covestro Deutschland AG filed Critical Covestro Deutschland AG
Publication of EP4347677A1 publication Critical patent/EP4347677A1/fr
Pending legal-status Critical Current

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Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the alkali- or alkaline earth metals or beryllium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/62—Preparation of compounds containing amino groups bound to a carbon skeleton by cleaving carbon-to-nitrogen, sulfur-to-nitrogen, or phosphorus-to-nitrogen bonds, e.g. hydrolysis of amides, N-dealkylation of amines or quaternary ammonium compounds
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
    • C08G18/30—Low-molecular-weight compounds
    • C08G18/32—Polyhydroxy compounds; Polyamines; Hydroxyamines
    • C08G18/3225—Polyamines
    • C08G18/3237—Polyamines aromatic
    • C08G18/324—Polyamines aromatic containing only one aromatic ring
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
    • C08G18/40—High-molecular-weight compounds
    • C08G18/48—Polyethers
    • C08G18/4804—Two or more polyethers of different physical or chemical nature
    • C08G18/4816—Two or more polyethers of different physical or chemical nature mixtures of two or more polyetherpolyols having at least three hydroxy groups
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
    • C08G18/40—High-molecular-weight compounds
    • C08G18/48—Polyethers
    • C08G18/50—Polyethers having heteroatoms other than oxygen
    • C08G18/5021—Polyethers having heteroatoms other than oxygen having nitrogen
    • C08G18/5024—Polyethers having heteroatoms other than oxygen having nitrogen containing primary and/or secondary amino groups
    • C08G18/5027—Polyethers having heteroatoms other than oxygen having nitrogen containing primary and/or secondary amino groups directly linked to carbocyclic groups
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/70—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the isocyanates or isothiocyanates used
    • C08G18/72—Polyisocyanates or polyisothiocyanates
    • C08G18/74—Polyisocyanates or polyisothiocyanates cyclic
    • C08G18/76—Polyisocyanates or polyisothiocyanates cyclic aromatic
    • C08G18/7657—Polyisocyanates or polyisothiocyanates cyclic aromatic containing two or more aromatic rings
    • C08G18/7664—Polyisocyanates or polyisothiocyanates cyclic aromatic containing two or more aromatic rings containing alkylene polyphenyl groups
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/70—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the isocyanates or isothiocyanates used
    • C08G18/72—Polyisocyanates or polyisothiocyanates
    • C08G18/74—Polyisocyanates or polyisothiocyanates cyclic
    • C08G18/76—Polyisocyanates or polyisothiocyanates cyclic aromatic
    • C08G18/7657—Polyisocyanates or polyisothiocyanates cyclic aromatic containing two or more aromatic rings
    • C08G18/7664—Polyisocyanates or polyisothiocyanates cyclic aromatic containing two or more aromatic rings containing alkylene polyphenyl groups
    • C08G18/7671—Polyisocyanates or polyisothiocyanates cyclic aromatic containing two or more aromatic rings containing alkylene polyphenyl groups containing only one alkylene bisphenyl group
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/82—Post-polymerisation treatment
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/14—Features of low-temperature carbonising processes
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G2110/00—Foam properties
    • C08G2110/0025—Foam properties rigid
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2375/00—Characterised by the use of polyureas or polyurethanes; Derivatives of such polymers
    • C08J2375/04—Polyurethanes

Definitions

  • the invention relates to a pyrolysis process for the thermal utilization of polyurethane-containing material, a corresponding use of a pyrolysis device and the product of the pyrolysis, which contains raw materials that can be recycled for the production of polyurethane.
  • Material containing polyurethane is used as padding or as insulating materials in the cooling and construction sectors.
  • foam-like polyurethane-containing materials are used, for example, as upholstery, mattresses, damping or insulation material.
  • polyurethane-containing materials as insulation, e.g. for refrigerators or in construction, rigid polyurethane foam is predominantly used.
  • plastic waste in landfills takes up a large volume and from there can also contribute to general pollution in rivers and seas. For this reason it is important to develop an efficient recycling method with which the waste problem can be solved and at the same time fossil resources can be saved.
  • the processes for recycling plastic waste can be roughly divided into 3 categories:
  • the chemical raw materials obtained from thermochemical recycling can be used to synthesize new synthetic resins or other chemical products.
  • Thermochemical recycling is called pyrolysis.
  • pyrolysis is applied to packaging waste and from it a pyrolysis oil is obtained, which is used as a type of recycled naphtha in the well-known refinery processes with crackers as drop in solution. Little is known about the pyrolysis of polyurethanes.
  • catalysts or additives in the pyrolysis process can lead to lower operating temperature, shorten reaction time, increase degradation efficiency and restrict product distribution, making the process more efficient.
  • DE 2410505 C2 describes a process for the thermal production of isocyanates from urethanes at 400° C. to 530° C. and reduced pressure. Experiments with polyurethanes under atmospheric pressure are not mentioned.
  • DE 2362915 proposes the hydrolysis of flexible polyurethane foam to form diamines in a fluidized bed.
  • Pyrolysis product should be obtained from polyurethane-containing materials in a targeted manner, which product contains a high content of cleavage products that can be reused for polyurethane synthesis, in particular aromatic amine compounds such as aniline, toluidine, methylenedianiline (mMDA) or polymeric methylenedianiline (pMDA).
  • aromatic amine compounds such as aniline, toluidine, methylenedianiline (mMDA) or polymeric methylenedianiline (pMDA).
  • aromatic isocyanate e.g. methylenediphenyl isocyanate (MDI) or polymeric methylenediphenyl-isocyanate (pMDI)
  • MDI methylenediphenyl isocyanate
  • pMDI polymeric methylenediphenyl-isocyanate
  • One subject of the present application is therefore a method for pyrolysis, comprising at least the following steps
  • Q is a hydrocarbon radical having 8 to 70 carbon atoms, preferably 10 to 30 carbon atoms, and n is a number from 2 to 10, preferably from 2 to 6, particularly preferably from 2 to 4 and -* means a covalent bond to the polymer backbone, and ii) at least one catalyst affecting the thermal decomposition of said polymeric compound, in a reactor;
  • step (b) decomposition of at least the material of the pyrolysis material introduced in step (a) in the reactor at a temperature of 250° C. to 700° C. to obtain product in the gas phase as pyrolysate and pyrolysis residue not in the gas phase, wherein
  • the amount of oxygen gas in the reactor is at most 2.0% by volume based on the total volume of gases in the reactor
  • pyrolysis material All of the substances introduced into the reactor for pyrolysis, which are thermally treated there in the absence of oxygen gas or in the presence of a reduced amount of oxygen gas, are referred to as "pyrolysis material". Before being introduced into the reactor, the pyrolysis material is preferably in solid form.
  • “Pyrolyzate” is understood as meaning all those products formed by pyrolysis which are in the gas phase of the reactor under the conditions of step (b) (in particular as a gas and/or as an aerosol).
  • “Pyrolysis residue” is understood to mean all those substances formed by pyrolysis and the other residues of the pyrolysis material which are not in the gas phase of the reactor under the conditions of step (b). Those embodiments of the process which are characterized in that the pyrolysis residue in the reactor is solid are preferred.
  • “Pyrolysis product” is understood to mean all those products from the pyrolysate that are obtained in step (c) during the cooling of the pyrolysate by condensation and/or resublimation. Pyrolysis product that is liquid is also known as pyrolysis oil.
  • a substance e.g. material, pyrolysis product, pyrolysate, pyrolysis product, pyrolysis residue
  • liquid if it is in the liquid state at 20°C and 1013 mbar.
  • solid if it is in the solid state of aggregation at 20°C and 1013 mbar.
  • a substance e.g. material, pyrolysis product, pyrolysate, pyrolysis residue
  • a substance is "gaseous” if it is present as a gas at 20°C and 1013 mbar im.
  • a substance is "organic” if its chemical structure contains at least one covalent carbon-hydrogen bond.
  • a “reactor” is a volume in which a chemical conversion, e.g. thermal decomposition of material from the pyrolysis material, takes place.
  • a chemical conversion e.g. thermal decomposition of material from the pyrolysis material
  • thermal decomposition for example, this can be the volume of a heated vessel in which the pyrolysis material is located.
  • a reactor according to the method according to the invention which is characterized in that it is selected from a continuous stirred tank reactor (CSTR), fixed bed reactor, fluidized bed reactor, screw reactor, screw conveyor reactor, entrained flow reactor, entrainment flow reactor, rotary tube reactor, fluidized bed reactor, paddle reactor.
  • CSTR continuous stirred tank reactor
  • those reactors are preferably suitable in which the pyrolysis material can be introduced continuously and are selected in particular from rotary tube reactors, continuous stirred tank reactors (CSTR), fixed bed reactors (in particular with continuous bed exchange (shaft reactor) with an internal heat exchanger, preferably with internal heat exchanger tubes, screw reactor, screw conveyor reactor, Entrained flow reactor, rotary tube reactor or fluidized bed reactor.
  • CSTR continuous stirred tank reactors
  • a very particularly preferred reactor of an embodiment of the Process is selected from screw reactor, rotary kiln or fluidized bed.
  • Further reactors preferred for the process according to the invention and their embodiments are described in the context of the embodiments of the device for pyrolysis according to the invention and in the context of an embodiment of the process using a catalyst (many below).
  • the pyrolysis material introduced into the reactor comprises at least one material containing at least one polymeric compound having at least one polyurethane structural unit of the formula (I), wherein
  • Q is a hydrocarbon radical having 8 to 70 carbon atoms, preferably 10 to 30 carbon atoms, and n is a number from 2 to 10, preferably from 2 to 6, particularly preferably from 2 to 4, and -* is a covalent bond to the polymer backbone.
  • Q is preferably derived from aliphatic hydrocarbon units, cycloaliphatic hydrocarbon units, araliphatic hydrocarbon units, aromatic hydrocarbon units or heterocyclic hydrocarbon units.
  • the method according to the invention is particularly suitable for those materials which contain said polymeric compound which, according to formula (I), has a group Q with at least one aromatic radical.
  • Very particularly preferred structural units of the formula (I) are those in which the group Q contains at least two alkylene-bridged aromatic radicals, preferably at least two alkylene-bridged phenyl radicals, in particular at least two methylene-bridged phenyl radicals.
  • a very particularly preferred embodiment of the process according to the invention is characterized in that the polymeric compound contains at least one polyurethane structural unit of the formula (Ia) as at least one structural unit of the aforementioned formula (I).
  • n is a number from 0 to 8, in particular from 0 to 4, more preferably from 0 to 2, and - * is a covalent bond to the polymer backbone.
  • the polymeric compound contained in said material can preferably be obtained by reacting at least i 1) at least one organic isocyanate compound containing at least two to ten, in particular two to eight, more preferably two to four, isocyanate groups binding to a hydrocarbon unit having 8 to 70 carbon atoms, preferably having 10 to 30 carbon atoms; with i2) at least one organic compound having at least two hydroxy groups.
  • the at least one organic isocyanate compound contains, as said hydrocarbon unit, a unit which has the number of carbon atoms mentioned in ii) and is derived from aliphatic hydrocarbon units, cycloaliphatic hydrocarbon units, araliphatic hydrocarbon units, aromatic hydrocarbon units or heterocyclic hydrocarbon units.
  • At least one compound of the formula (II) is particularly preferably selected as said organic isocyanate compound
  • Q is a radical selected from an aliphatic hydrocarbon radical having 8 to 70 carbon atoms, preferably having 10 to 30 carbon atoms, a cycloaliphatic hydrocarbon radical having 8 to 70 carbon atoms, preferably having 10 to 30 carbon atoms, an aromatic hydrocarbon radical having 8 to 70 carbon atoms, preferably having 10 to 30 carbon atoms, or an araliphatic hydrocarbon radical having 8 to 70 carbon atoms with 10 to 30 carbon atoms.
  • polymeric compound contains at least one structural unit of the aforementioned formula (Ia) embodiment, it has proven to be a further preferred embodiment of the process if at least one polyphenylpolymethylene polyisocyanate of the formula (III) is selected as at least one organic polyisocyanate compound in step il), where n is a number from 0 to 8, in particular from 0 to 4, more preferably from 0 to 2.
  • At least one organic compound having at least two hydroxyl groups is selected from polyester polyol, polyether polyol, polycarbonate polyol, polyether ester polyol, polyacrylate polyol, polyester polyacrylate polyol or mixtures thereof.
  • At least one organic compound having at least two hydroxyl groups is preferably selected from the group of polyether polyols and/or polyester polyols.
  • the OH number of the polyol or polyols used can be, for example, >100 mg KOH/g to ⁇ 800 mg KOH/g and the average OH functionality of the polyol or polyols used is >2.
  • the OH number gives in the case of a single polyol added, its OH number. In the case of mixtures, the average OH number is given. This value can be determined using DIN 53240.
  • the average OH functionality of the polyols is, for example, in a range from >2 to ⁇ 6.
  • polyether polyols which can be used are polytetramethylene glycol polyethers, as can be obtained by polymerizing tetrahydrofuran by means of cationic ring opening.
  • suitable polyether polyols are addition products of styrene oxide, ethylene oxide, propylene oxide, butylene oxides and/or epichlorohydrin onto difunctional or polyfunctional starter molecules.
  • Polyether polyols with ethylene oxide or propylene oxide as chain extenders are mostly used.
  • Suitable starter molecules are, for example, ethylene glycol, diethylene glycol, butyl diglycol, glycerol, diethylene glycol, trimethylolpropane, propylene glycol, pentaerythritol, sorbitol, sucrose, ethylenediamine, toluenediamine, triethanolamine, 1,4-butanediol, 1,6-hexanediol and low molecular weight, hydroxyl-containing esters of such polyols with dicarboxylic acids.
  • Polyester polyols that can be used include polycondensates of di- and also tri- and tetracarboxylic acids and di- and also tri- and tetracarboxylic acids
  • Suitable diols are ethylene glycol, butylene glycol, diethylene glycol, triethylene glycol, polyalkylene glycols such as polyethylene glycol, also 1,2-propanediol, 1,3-propanediol, 1,3-butanediol, 1,3-butanediol, 1,6-hexanediol and isomers, neopentyl glycol or
  • polyols such as trimethylolpropane, glycerol, erythritol, pentaerythritol, trimethylolbenzene or trishydroxyethyl isocyanurate can also be used.
  • polycarboxylic acids which can be used are phthalic acid, isophthalic acid, terephthalic acid, tetrahydrophthalic acid, hexahydrophthalic acid, cyclohexanedicarboxylic acid, adipic acid, azelaic acid, sebacic acid, glutaric acid, tetrachlorophthalic acid, maleic acid, fumaric acid, itaconic acid, malonic acid, suberic acid, succinic acid, 2-methylsuccinic acid, 3,3-diethylglutaric acid, 2 ,2-dimethylsuccinic acid, dodecanedioic acid, endomethylenetetrahydrophthalic acid, dimer fatty acid, trimer fatty acid, citric acid or trimellitic acid can be used.
  • the corresponding anhydrides can also be used as the acid source. If the average functionality of the polyol to be esterified is >2, monocarboxylic acids such as benzoic acid and
  • hydroxycarboxylic acids which can be used as reactants in the preparation of a hydroxyl-terminated polyester polyol are hydroxycaproic acid, hydroxybutyric acid, hydroxydecanoic acid, hydroxystearic acid and the like.
  • Suitable lactones include caprolactone, butyrolactone and homologues.
  • Polycarbonate polyols which can be used are polycarbonates containing hydroxyl groups, for example polycarbonate diols. These can be obtained by reacting carbonic acid derivatives, such as diphenyl carbonate, dimethyl carbonate or phosgene, with polyols, preferably diols, or from carbon dioxide.
  • diols examples include ethylene glycol, 1,2- and 1,3-propanediol, 1,3- and 1,4-butanediol, 1,6-hexanediol, 1,8-octanediol, neopentyl glycol, 1,4-bishydroxymethylcyclohexane, 2 -Methyl-1,3-propanediol, 2,2,4-trimethylpentanediol-1,3, dipropylene glycol, polypropylene glycols, dibutylene glycol, polybutylene glycols, bisphenol A and lactone-modified diols of the type mentioned above.
  • polyether polycarbonate diols can also be used be used.
  • Polyetherester polyols which can be used are those compounds which contain ether groups, ester groups and OH groups.
  • Organic dicarboxylic acids with up to 12 carbon atoms are suitable for preparing the polyetherester polyols, preferably aliphatic dicarboxylic acids with >4 to ⁇ 6 carbon atoms or aromatic dicarboxylic acids, which are used individually or in a mixture.
  • Examples include suberic acid, azelaic acid, decanedicarboxylic acid, maleic acid, malonic acid, phthalic acid, pimelic acid and sebacic acid and, in particular, glutaric acid, fumaric acid, succinic acid, adipic acid, phthalic acid, terephthalic acid and isoterephthalic acid.
  • Derivatives of these acids which can be used are, for example, their anhydrides and their esters and half-esters with low molecular weight, monofunctional alcohols having >1 to ⁇ 4 carbon atoms.
  • the at least one organic compound having at least two hydroxyl groups is preferably at least one aliphatic polyester polyol which, in addition to structural units derived from adipic acid, also contains structural units derived from glutaric acid, succinic acid and/or phthalic acid, preferably glutaric acid and/or succinic acid.
  • the polymeric compound of the material can optionally additionally contain isocyanurate structural units of the formula included, wherein R is a divalent hydrocarbon radical, in particular a divalent aromatic hydrocarbon radical. For this embodiment, it has proven to be preferred if the proportion of these isocyanurate structural units in the total weight of the material is at most 40% by weight.
  • said pyrolysis product contains said polyurethane polymer-containing material in a total amount of 10.0 to 80.0% by weight, more preferably 30.0 to 70.0% by weight, in each case based on the total weight of the pyrolysis material.
  • the material containing said polymeric compound is a foam, more preferably a polyurethane foam.
  • the material is in the form of a polyurethane foam, it is again preferably a flexible polyurethane foam or a rigid polyurethane foam.
  • a rigid polyurethane foam is a very particularly preferred embodiment of the material introduced into the pyrolysis material in step a) of the method.
  • the said material is in the form of a rigid polyurethane foam, it has proven to be advantageous if the rigid polyurethane foam according to DIN 7726: 1982-05 has a compressive stress of >15 kPa under pressure with 10% compression, measured according to DIN 53421.
  • said material of the pyrolysis material is preferably introduced into the reactor in the form of solid particles (in particular in the form of a granular mixture).
  • a granular mixture of said material is formed from a multitude of loose, solid particles of said material, which in turn are called granules include.
  • a grain is a designation for the particulate components of powders (grains are the loose, solid particles), dusts (grains are the loose, solid particles), granules (loose, solid particles are agglomerates of several grains) and other granular mixtures.
  • the flowability of a granular mixture relates to its ability to flow freely under its own weight from a flow test funnel with a 16.5 mm diameter outlet.
  • the solid particles, in particular the loose, solid particles of the granular mixture, of said material introduced into the reactor preferably have an average diameter X o (volume average) of 0.01 mm to 5 cm, preferably 0.1 mm to 5 cm. on.
  • the average particle size diameter Xso is determined by sieving or using a particle size analyzer Camsizer from Retsch.
  • the dosing and processability of the pyrolysis material in the pyrolysis of the method according to the invention can be simplified by said pyrolysis material in step (a) additionally containing at least one filler in addition to said material.
  • Said filler preferably does not catalyze the thermal decomposition of polyurethane as part of the pyrolysis. It is in turn particularly preferred if the filler is at least one metal oxide which is not catalytically active in the pyrolysis of the thermal decomposition of polyurethane, which is preferably selected from SiCh.
  • Said material is preferably mixed with a filler, e.g. sand, which simplifies continuous process management of the method according to the invention. In particular, sticking of said material in the reactor and in the supply of the dosing device to the reactor is avoided.
  • the filler and said material are added to the pyrolysis material as a mixture in a volume ratio of filler to said material of at least 0.1:1 to 10:1.
  • the pyrolysis must contain at least one catalyst. This catalyst affects the reaction of decomposition of said material.
  • a suitable catalyst can lower the pyrolysis temperature, reduce the product range to the desired products and, if necessary, minimize coking. Inexpensive catalysts are preferred for an efficient process.
  • Naturally occurring materials such as inorganic salts, refractory oxides, minerals, and engineered rocks, into which ions can optionally be exchanged in a simple ion exchange process, can act as effective catalysts because they do not require extensive synthesis. They are readily available and are therefore relatively cheap.
  • synthetic catalysts such as zeolites (ZSM-5, ZeoliteX,Y, etc) are an example of catalysts that are effective but not cheap as they have to be specially manufactured.
  • catalysts can also simplify the dosing and processability of the pyrolysis material in pyrolysis. If a catalyst is used, the amount of filler used can be reduced in this case. In one embodiment, the total amount of filler and catalyst is fed to the pyrolysis material as a mixture in relation to the amount of said material in a volume ratio of at least 0.1:1 to 10:1.
  • the pyrolysis material can contain at least one basic catalyst. If it is a solid, basic catalyst, the number and strength of the basic centers of the catalyst can be determined using Fourier transform infrared spectroscopy and Temperature Programmed Desorption of CO2 (TPD-C02), or using common titrimetric methods.
  • At least one catalyst is selected from the group formed by alkaline inorganic materials, more preferably from the group of naturally occurring materials defined above.
  • These inorganic materials can be refractory oxides.
  • Refractory oxides are metal oxides that are stable at high temperatures from 300°C to 700°C.
  • Such catalyst oxides include the oxides of aluminum, magnesium, zirconium, titanium, chromium, zinc, tin and other metals or combinations of alumina with magnesium oxide and/or with calcium oxide.
  • Crystalline inorganic materials include aluminosilicates, silicoaluminophosphates, silicalite, spinels and other natural zeolites and clays. At least one compound from the group consisting of inorganic salts, minerals, metal oxides, mixed oxides, clays and zeolites is therefore particularly suitable as said catalyst.
  • the catalyst particularly preferably contains at least one oxide of aluminum in the form of an oxide or mixed oxide and has a spinel structure, hydrotalcite structure or y-Ah0 3 structure.
  • a mixed oxide of Al2O3 and MgO is particularly suitable as a catalyst. This in turn is very particularly preferably present in a spinel structure or hydrotalcite structure.
  • Both homogeneous and heterogeneous catalysts can be used.
  • preferred embodiments of the process according to the invention are those in which the catalyst is a heterogeneous catalyst.
  • the catalyst is preferably introduced into the reactor in the form of solid particles (in particular in the form of a granular mixture).
  • the heterogeneous catalyst used particularly preferably has an average particle size of its solid particles, in particular its loose, solid particles of the granular mixture, an average diameter X50.3 (volume average) of 0.01 mm to 5 cm, preferably from 0.1 mm to 5 cm, on.
  • the average particle size diameter X50.3 is determined by sieving or using a particle size analyzer Camsizer from Retsch.
  • the catalyst particles have a smaller or the same particle size as the particles of said material. It is therefore preferred if the mean particle size of the catalyst present in the pyrolysis material corresponds at most to the mean particle size of the said material present therein.
  • a catalyst If a catalyst is added, it can be admixed with the filler, coated onto the filler, or used as a substitute for the filler.
  • the catalyst used in the process according to the invention tends to get deposits of coke and other carbon residues
  • a reactor which allows the catalyst to be discharged easily and preferably and continuously regenerated. Therefore, the use of a continuous stirred tank reactor (CSTR), a moving bed, a screw reactor, a screw conveyor reactor, an entrained flow reactor, a rotating cone reactor, or a fluidized bed reactor is preferred over the use of a fixed bed reactor.
  • the (eg by coking) deactivated catalyst is in the pyrolysis residue and can be fed into a regenerator after the pyrolysis residue has been discharged from the reactor and added to the pyrolysis material of step (b) to be introduced into the pyrolysis reactor after regeneration.
  • Reactors that allow for short contact time, intensive mixing of the components in the feedstream with the catalyst, and continuous recycle of the regenerated catalyst to the pyrolysis zone are most preferred. Since this is the case with a screw reactor, rotary kiln or fluidized bed, these reactors are particularly preferred.
  • the pyrolysis material introduced into the reactor in step (a) is at least partially decomposed in step (b) with the formation of pyrolysate and pyrolysis residue.
  • the pyrolysis material After being introduced into the reactor, the pyrolysis material is heated to a temperature in the range from 250.degree. C. to 700.degree.
  • a particularly successful improvement in the result of the method according to the invention can be achieved if, within the scope of one embodiment, the pyrolysis material introduced is heated to 250° C. to 700° C. and, after this target temperature has been reached, the residence time of the correspondingly temperature-controlled pyrolysis material is increased until the resulting pyrolysis residue is discharged 1 second to 2 hours, preferably between 2 minutes and 60 minutes, and during which time the temperature and the content of oxygen gas in the reactor are the values defined in step (b).
  • the pyrolysis material contains a catalyst in the process according to the invention, this catalyst is present in the pyrolysis residue that is discharged. As part of a further embodiment of the method, the discharged pyrolysis residue is therefore fed to a regeneration step of the catalyst contained therein, as described above.
  • step (b) good results can be achieved if the removal of the pyrolysate from the reactor that takes place in step (b) is ensured by a gas stream conducted through the reactor or by suction and more preferably by allowing the pyrolysate to remain there as a period of time between the point in time at which the said material introduced into the reactor in step (a) and the point in time at which the pyrolysate is discharged is 0.1 seconds to 600 seconds, preferably between 0.5 seconds and 300 seconds, particularly preferably 0.5 seconds to 200 seconds. If a gas stream is passed through the reactor for this purpose, an inert gas, preferably selected from nitrogen, argon, CO 2 , NO or a mixture thereof, is particularly suitable as the gas for this gas stream.
  • an inert gas preferably selected from nitrogen, argon, CO 2 , NO or a mixture thereof, is particularly suitable as the gas for this gas stream.
  • the flow velocity of the gas stream in the reactor is in the range from 0.01 m/s to 20 m/s as superficial velocity. If a fixed-bed reactor is chosen as the reactor, it is preferred according to the invention if the flow rate of the gas stream in the reactor is in the range from 0.03 m/s to 1 m/s as the superficial velocity. If a fluidized bed reactor is selected as the reactor, it is preferred according to the invention that the superficial velocity of the gas stream in the reactor is in the range from 0.5 m/s to 2 m/s. If an entrained-flow reactor is selected as the reactor, it is preferred according to the invention that the superficial velocity of the gas stream in the reactor is in the range from 5 m/s to 20 m/s.
  • the temperature in the reactor is from 250 to 700° C. and the amount of oxygen gas in the reactor is from 0 to 2.0% by volume based on the total volume in the reactor gases.
  • the reactor filled with said material of said pyrolysis material is filled with inert gas, in particular with nitrogen, argon, CO2, NO or a mixture thereof.
  • Reactive gases other than oxygen gas can also be added to the inert gas, in particular selected from methane, gaseous H2O, hydrogen gas or mixtures thereof.
  • the pyrolysis material can be freed from oxygen gas before it is introduced in step (a), e.g. by driving out the oxygen gas by means of stripping with a stripping gas, e.g. in one upstream of the reactor storage container.
  • a stripping gas e.g. in one upstream of the reactor storage container.
  • inert gas in particular nitrogen, argon, CO2, NO, mixtures thereof, could be used as a stripping gas from above or below in the storage container (preferably from above) via a frit into the container to the pyrolysis material in order to drive out the oxygen gas.
  • the absolute pressure in step (b) is at most 1.2 bar.
  • the temperature in step (b) is from 300.degree. C. to 700.degree. C., preferably from 400.degree. C. to 600.degree.
  • the amount of oxygen gas in the reactor in step (b) is at most 0.5% by volume, preferably at most 0.1% by volume, based in each case on the total volume of the gases in the reactor.
  • step (b) the temperature is firstly from 300° C. to 700° C., more preferably from 400° C. to 600° C., and secondly the amount of oxygen gas in the reactor is at most 0, 5% by volume, preferably at most 0.1% by volume, in each case based on the total volume of the gases present in the reactor. It is again extremely preferred if, thirdly, the absolute pressure in step (b) is at most 1.2 bar.
  • a preferred embodiment of the method provides a continuous process control. For this, at least steps (a) and (b) run simultaneously within the framework of a continuous process control.
  • the pyrolysis product obtained in step (c) can be worked up using standard separation methods, for example distillation or selective condensation, and (i) can thereby be obtained.
  • the method according to the invention can be carried out with the aid of an appropriately configured pyrolysis device.
  • Another object of the invention is therefore the use of a pyrolysis device containing at least one dosing device for feeding in pyrolysis material, at least one heatable reactor for pyrolysis, and at least one pyrolysate collector, said heatable reactor for pyrolysis containing at least one heating element for temperature control the reactor can be used at a temperature of 250°C to 700°C, and contains at least one inlet for pyrolysis material and at least one outlet for pyrolysate different therefrom; and
  • Metering device and heatable reactor for the pyrolysis are arranged and designed relative to each other in such a way that the metering device is connected via at least one feed line to an inlet for pyrolysis material of said reactor; and the heatable reactor for the pyrolysis and the pyrolysate collector are in fluid communication with one another, so that the preferably gaseous pyrolysate can be discharged from said pyrolysate outlet and the pyrolysate discharged can be introduced into the pyrolysate collector; and at least one pyrolysate collector contains at least one cooling device conditioned to a temperature below 250°C, which is installed in said collector to lower the temperature of the pyrolysate fed out of said reactor to less than 250°C to form a pyrolysis product selected from pyrolysate condensate, pyrolysate sublimate or a mixture thereof, and comprising at least one container for collecting and discharging the product of pyrolysis obtained with cooling; and at least
  • Q is a hydrocarbon radical having 8 to 70 carbon atoms and n is a number from 2 to 10, preferably from 2 to 6, particularly preferably from 2 to 4, and -* is a covalent bond to the polymer backbone.
  • polymeric compounds mentioned in the context of the description of the process also apply as preferred polymeric compounds for the pyrolysis.
  • said pyrolysis device for recovering at least one aromatic amino compound having at least one amino group, in particular selected from aniline, toluidine, methylenedianiline (mMDA), polymeric methylenedianiline (pMDA) or mixtures thereof.
  • mMDA methylenedianiline
  • pMDA polymeric methylenedianiline
  • a heating element e.g. heating coil or heating plates, can be used to heat the heatable reactor of said pyrolysis device, for example, or a device for heating a gas stream and for introducing the heated gas stream into the reactor.
  • the reactor additionally contains at least one connection to a gas source, with a gas stream in the reactor, preferably with a flow rate as superficial tube rate of between 0.01 m/s and 20 m/s, being controlled via a control, e.g. a valve. flows through the reactor into the pyrolysate collector.
  • a control e.g. a valve.
  • the flow rate of the gas stream in the reactor is in the range from 0.03 m/s to 1 m/s as the superficial velocity.
  • a fluidized bed reactor is selected as the reactor, it is preferred according to the invention that the superficial velocity of the gas stream in the reactor is in the range from 0.5 m/s to 2 m/s.
  • the superficial velocity of the gas stream in the reactor is in the range from 5 m/s to 20 m/s.
  • the gas stream from the gas source can, for example, be heated by the heater before it is introduced into the reactor, as described above.
  • the pyrolysate collector of the pyrolysis device preferably contains a cooling device usable in said collector for lowering the temperature of the pyrolysate discharged from said reactor to less than 50°C (more preferably less than 30°C) to form pyrolysis product. Cooling units that work according to the heat exchanger principle are particularly suitable for this.
  • the pyrolysate collector can be equipped as a selective condenser for a selective condensation of pyrolysis product components contained in the pyrolysate.
  • a “fluid connection” is a part of the device that connects parts of the system to one another and through which a substance that can be present in any physical state can be transported from one part of the system to the next, for example a supply line in the form of a pipe.
  • the method according to the invention and the device according to the invention contribute to the solution of the object set out above and, after step (c) of the method, deliver as a pyrolysis product a composition containing at least one based on the total weight of the composition
  • the composition contains under (i) from 0 to 40% by weight of the compound of the formula (IV) where n is a number from 0 to 8, in particular from 0 to 4, more preferably from 0 to 2.
  • More preferred pyrolysis products contain more (i) aromatic compounds having at least two amino groups than (ii) aromatic compounds having exactly one amino group.
  • the composition under (ii) contains between 0 and 35% by weight of a total amount of aromatic amino compound having at least one amino group selected from aniline, toluidine or mixtures thereof.
  • the pyrolysis product contains between 0 and 40% by weight of a total amount of at least one aromatic compound having at least two amino groups.
  • the composition under (iii) contains between 0 and 40% by weight of hydrocarbon compounds containing at least one functional group with at least one oxygen atom and no functional group with nitrogen atom.
  • hydrocarbon compounds are in turn particularly preferably selected from compounds with a molar mass of at most 300 g/mol, in particular at most 250 g/mol. More preferably, said hydrocarbon compounds are selected from acetone, dimethyldioxane, propene, 1,2-propylene glycol, dipropylene glycol, tripropylene glycol or tetrapropylene glycol.
  • Process for pyrolysis comprising at least the following steps (a) introduction of pyrolysis material, comprising at least i) material containing at least one polymeric compound having at least one polyurethane structural unit of the formula (I), wherein
  • Q is a hydrocarbon radical having 8 to 70 carbon atoms, preferably 10 to 30 carbon atoms, and n is a number from 2 to 10, preferably from 2 to 6, particularly preferably from 2 to 4, and -* is a covalent bond to the polymer backbone, and ii) at least one catalyst affecting the thermal decomposition of said polymeric compound in a reactor;
  • step (b) decomposition of at least the material of the pyrolysis material introduced in step (a) in the reactor at a temperature of 250° C. to 700° C. to obtain product in the gas phase as pyrolysate and pyrolysis residue not in the gas phase, wherein (i) during said decomposition, the amount of oxygen gas in the reactor is at most 2.0% by volume based on the total volume of gases in the reactor, and
  • CSTR continuous stirred tank reactor
  • fixed bed reactor fixed bed reactor
  • fluidized bed reactor fluidized bed reactor
  • Screw reactor screw conveyor reactor, entrained flow reactor, rotary tube reactor, paddle reactor, in particular selected from continuous stirred tank reactor (CSTR), fixed bed reactor (in particular with continuous bed exchange (shaft reactor) preferably with internal heat exchanger tubes), a screw reactor, a screw conveyor reactor, an entrained flow reactor, rotary tube reactor or fluidized bed reactor.
  • CSTR continuous stirred tank reactor
  • shaft reactor fixed bed reactor (in particular with continuous bed exchange (shaft reactor) preferably with internal heat exchanger tubes)
  • a screw reactor a screw conveyor reactor, an entrained flow reactor, rotary tube reactor or fluidized bed reactor.
  • the absolute pressure in step (b) is at most 1.2 bar.
  • the pyrolysis material introduced is heated to 250°C to 700°C and, after this target temperature has been reached, the residence time of the correspondingly temperature-controlled pyrolysis material up to the point at which its resulting pyrolysis residue is discharged is preferably 1 second to 5 hours between 2 minutes and 120 minutes.
  • Method characterized in that the removal of the pyrolysate from the reactor is ensured by a gas stream guided through the reactor or by suction and preferably thereby a residence time of the pyrolysate as a period between the time of the formation of the pyrolysate and the time of the Ejection of the resulting pyrolysate from the reactor 0.1 seconds to 600 seconds, preferably between 0.5 seconds and 300 seconds, particularly preferably 0.5 seconds to 200 seconds.
  • the method according to any one of the preceding aspects, characterized in that the evacuation of the pyrolyzate from the reactor is ensured by a guided through the reactor gas flow, the flow rate in the reactor as
  • empty pipe velocity is in the range of 0.01 m/s to 20 m/s.
  • Process according to one of the preceding aspects characterized in that the pyrolysis residue in the reactor is solid.
  • Method according to one of the preceding aspects characterized in that at least steps (a) and (b) run simultaneously as part of a continuous process control.
  • Process according to one of the preceding aspects characterized in that in step (b) the amount of oxygen gas in the reactor is at most 0.5% by volume, preferably at most 0.1% by volume, based in each case on the total volume of the gases in the reactor .
  • Method according to one of the preceding aspects characterized in that inert gas, in particular nitrogen, argon, CO2, NO or mixtures thereof, flows through the reactor filled with said material.
  • Method according to aspect 11 characterized in that reactive gases different from oxygen gas are admixed to the inert gas, in particular selected from methane, gaseous H2O, hydrogen gas or mixtures thereof.
  • the polymeric compound of the polyurethane material additionally has isocyanurate structural units of the formula contains, wherein R is a divalent hydrocarbon radical, in particular a divalent aromatic hydrocarbon radical.
  • the polymeric compound contains at least one polyurethane structural unit of the formula (Ia). where n is a number from 0 to 8, in particular from 0 to 4, more preferably from 0 to 2, and -* is a covalent bond to the polymer backbone.
  • the polymeric compound by reacting at least i 1) at least one organic isocyanate compound containing at least two to ten, in particular two to eight, more preferably two to four, isocyanate groups binding to a hydrocarbon unit with 8 to 70 carbon atoms, preferably with 10 to 30 carbon atoms; with i2) at least one organic compound having at least two hydroxy groups.
  • Isocyanate compound contains as said hydrocarbon moiety a moiety having the aforementioned number of carbon atoms and derived from aliphatic hydrocarbon moieties, cycloaliphatic hydrocarbon moieties, araliphatic hydrocarbon moieties, aromatic hydrocarbon moieties or heterocyclic hydrocarbon moieties.
  • At least one organic compound having at least two hydroxyl groups is selected from polyester polyol, polyether polyol, polycarbonate polyol, polyether ester polyol, polyacrylate polyol, polyester polyacrylate polyol or mixtures thereof, preferably at least one aliphatic polyester polyol, which in addition to adipic acid derived structural units also contains structural units derived from glutaric acid, succinic acid and/or phthalic acid, preferably glutaric acid and/or succinic acid. 21.
  • the material is present as a rigid polyurethane foam in the pyrolysis material, preferably as a rigid polyurethane foam which, according to DIN 7726: 1982-05, has a compressive stress of >15 kPa when subjected to a compressive load at 10% compression, measured according to DIN 53421. 22.
  • the material is present as a rigid polyurethane foam in the pyrolysis material, preferably as a rigid polyurethane foam which, according to DIN 7726: 1982-05, has a compressive stress of >15 kPa when subjected to a compressive load at 10% compression, measured according to DIN 53421.
  • Material in the form of solid particles, in particular in the form of a granular mixture, is introduced into the reactor.
  • the catalyst is at least one compound from the group consisting of inorganic salts, minerals, metal oxides, mixed oxides, clays, zeolites, preferably a mixed oxide of Al2O3 and MgO.
  • Pyrolysis material contains said material in a total amount of 10.0 to 80.0% by weight, more preferably 30.0 to 70.0% by weight, based on its total weight.
  • a pyrolysis device containing at least one dosing device for feeding in pyrolysis material, at least one heatable reactor for the pyrolysis, and at least one pyrolysate collector
  • said heatable reactor for the pyrolysis containing at least one heating element, which is used to control the temperature of the reactor to a temperature of 250°C to 700°C can be used, and contains at least one inlet for pyrolysis material and contains at least one different outlet for pyrolysate
  • Metering device and heatable reactor for the pyrolysis are arranged and designed relative to each other in such a way that the metering device is connected via at least one feed line to an inlet for pyrolysis material of said reactor; and the heatable reactor for the pyrolysis and the pyrolysate collector are in fluid communication with one another, so that the preferably gaseous pyrolysate can be discharged from said pyrolysate outlet and the pyrolysate discharged can be introduced into the pyro
  • Q is a hydrocarbon radical having 8 to 70 carbon atoms and n is a number from 2 to 10, preferably from 2 to 6, particularly preferably from 2 to 4, and -* is a covalent bond to the polymer backbone.
  • the pyrolysis device for the recovery of at least one aromatic amino compound with at least an amino group in particular selected from aniline, toluidine, methylenedianiline (mMDA), polymeric methylenedianiline (pMDA) or mixtures thereof.
  • a rigid polyurethane foam was produced from the components shown in Table 1 using standard methods.
  • pyrolysis material P4 contained no catalyst.
  • the pyrolysis of the rigid polyurethane foam was carried out at 500° C. in a fixed bed reactor with a volume of 25 ml through which N2 flowed.
  • the flow rate of the nitrogen gas stream (superficial velocity) in the reactor was 0.07 m/s.
  • a material for pyrolysis according to Table 1 was introduced into the reactor. The residence time of the polyurethane material introduced was 30 minutes. The reactor was heated to 500° C. and then held at this temperature for 30 minutes. There were 3 condensers behind the reactor to separate the liquid components from the resulting pyrolysis gas. The proportion of coke formed was determined by weighing the catalyst powder after pyrolysis. The gas after the 3 condensers was characterized by online IR. The components in the pyrolysis product, which occurs as an oil, were determined using GC-FID. An Agilent 7890A with a Supelco SPB 50 column was used for this. The pyrolysis oil was diluted with acetone 1:50 or 1:100. Table 3: Composition of the pyrolysate obtained [% by weight]:

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Abstract

L'invention concerne un procédé selon la revendication 1 et des dispositifs de pyrolyse pour la pyrolyse d'une matière de pyrolyse comprenant une matière contenant du polyuréthane, permettant la mise en oeuvre de la pyrolyse à l'échelle industrielle. Selon l'invention, même avec des quantités plus élevées de matière de pyrolyse, on obtient une quantité de produit de pyrolyse qui contient des produits de clivage qui peuvent être réutilisés pour la synthèse d'une matière contenant du polyuréthane.
EP22731580.1A 2021-06-02 2022-06-01 Pyrolyse d'une matière contenant un composé de polyuréthane afin de récupérer des matières premières Pending EP4347677A1 (fr)

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PCT/EP2022/064853 WO2022253873A1 (fr) 2021-06-02 2022-06-01 Pyrolyse d'une matière contenant un composé de polyuréthane afin de récupérer des matières premières

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EP22731580.1A Pending EP4347677A1 (fr) 2021-06-02 2022-06-01 Pyrolyse d'une matière contenant un composé de polyuréthane afin de récupérer des matières premières

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WO2025202163A1 (fr) 2024-03-28 2025-10-02 Covestro Deutschland Ag Procédé et système pour obtenir de l'aniline
WO2025223981A1 (fr) 2024-04-25 2025-10-30 Covestro Deutschland Ag Procédé d'obtention d'aniline par clivage thermique d'uréthanes ou d'amines
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US3789278A (en) 1972-12-20 1974-01-29 Ibm Corona charging device
US3870739A (en) 1973-03-05 1975-03-11 Air Prod & Chem Isocyanates from urethanes
IT1109129B (it) * 1978-04-07 1985-12-16 Fiat Spa Procedimento per il trattamento degli scarti di poliuretano al fine del loro riutilizzo
US4365025A (en) * 1981-12-08 1982-12-21 W. R. Grace & Co. Flexible polyurethane foams from polymethylene polyphenyl isocyanate containing prepolymers
ATE241682T1 (de) * 1995-01-25 2003-06-15 O E T Calusco S R L Verfahren und einrichtung für die pyrolytische behandlung von organisches material enthaltenden abfällen, insbesondere die behandlung von hausmüll
AU704932B2 (en) * 1996-10-08 1999-05-06 Jong Han Jeon A method for preparation of recycled polyols and a method for manufacturing polyurethane foams with improved thermal insulation property
DE10130820A1 (de) * 2001-06-26 2003-01-02 Degussa Verfahren zur Spaltung von Polyurethanen
JP4601223B2 (ja) * 2001-09-13 2010-12-22 東洋ゴム工業株式会社 ポリウレタンの分解方法
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