EP4174150B1 - Verfahren zur behandlung von kunststoffabfällen - Google Patents

Verfahren zur behandlung von kunststoffabfällen Download PDF

Info

Publication number
EP4174150B1
EP4174150B1 EP21205587.5A EP21205587A EP4174150B1 EP 4174150 B1 EP4174150 B1 EP 4174150B1 EP 21205587 A EP21205587 A EP 21205587A EP 4174150 B1 EP4174150 B1 EP 4174150B1
Authority
EP
European Patent Office
Prior art keywords
lwp
stream
catalyst
hydrotreatment
fraction
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.)
Active
Application number
EP21205587.5A
Other languages
English (en)
French (fr)
Other versions
EP4174150A1 (de
Inventor
Antti Kurkijärvi
Marjut Aho
Jarmo Kela
Ville PAASIKALLIO
Emma SAIRANEN
Andrea PÉREZ NEBREDA
Jukka Keyriläinen
Perttu Uotila
Mika Kettunen
John Jamieson
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.)
Neste Oyj
Original Assignee
Neste Oyj
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=78414522&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP4174150(B1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Neste Oyj filed Critical Neste Oyj
Priority to EP21205587.5A priority Critical patent/EP4174150B1/de
Priority to ES21205587T priority patent/ES2992534T3/es
Priority to DK21205587.5T priority patent/DK4174150T3/da
Priority to FIEP21205587.5T priority patent/FI4174150T3/fi
Priority to HUE21205587A priority patent/HUE069562T2/hu
Priority to PL21205587.5T priority patent/PL4174150T3/pl
Priority to CA3235790A priority patent/CA3235790A1/en
Priority to US18/705,766 priority patent/US20250002798A1/en
Priority to PCT/EP2022/080245 priority patent/WO2023073194A1/en
Priority to KR1020247015111A priority patent/KR20240073975A/ko
Priority to MX2024004679A priority patent/MX2024004679A/es
Priority to JP2024525487A priority patent/JP2024541709A/ja
Publication of EP4174150A1 publication Critical patent/EP4174150A1/de
Publication of EP4174150B1 publication Critical patent/EP4174150B1/de
Application granted granted Critical
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

Definitions

  • the present invention relates to a method of treating waste plastic, especially liquified waste plastic treatment by hydrotreatment.
  • the method includes removal of impurities and hydrogenation of the LWP.
  • the method comprises two separate hydrotreatments of the LWP, where the second hydrotreatment is performed on a blend of hydrocarbons and already hydrotreated LWP.
  • Waste plastic is a growing environmental concern, since many of the polymers constituting the plastics are very stable and do not degrade in nature. Incineration of waste plastic increases greenhouse gases and also leads to other environmental concerns in the form of air and land pollution. Incineration of waste plastic is largely considered a waste of valuable raw material, even if the energy in form of heat is collected.
  • Plastics or polymers mainly constitute carbon, hydrogen and heteroatoms such as oxygen and/or nitrogen.
  • waste plastics also contain many impurities, such as metal and chlorine impurities.
  • impurities such as metal and chlorine impurities.
  • Fuels are mixtures of hydrocarbons, but production of liquid fuels from waste plastic is generally not considered useful.
  • Direct incineration of waste plastic also produces energy, which can be captured and used for heating and/or production of electricity etc. Therefore, there is a need to upgrade waste plastic to high end hydrocarbon components, which can be utilized in the production of new plastics, chemicals or other materials.
  • Waste plastics have been treated by pyrolysis to produce liquefied waste plastic (LWP), but the LWP feed still contains large amounts of various impurities and contaminants.
  • the LWP feed therefore needs to undergo various purification and pre-treatment steps before it can be used as feedstock for various upgrading processes.
  • Document WO2021/110395 describes a process for treating a feed comprising waste plastic pyrolysis oil, the process includes a hydrogenation step at a temperature of 100 °C to 250 °C, followed by a hydrotreatment step at a temperature of 250 °C to 430 °C.
  • the product thus obtained is further separated into a gaseous effluent, an aqueous effluent and a hydrocarbon effluent.
  • WO2021/204819 , FR3107530 and WO2021/105326 all disclose a method of processing LWP and the obtained product.
  • the current invention provides an improved process of treating and purifying LWP obtained e.g. through pyrolysis of waste plastic.
  • the present invention aims to provide an optimised solution for chemical recycling of waste plastics.
  • the invention strives to make chemical recycling a viable and economical and thereby a complementary solution to recycled waste plastic streams that are not suitable for mechanical recycling.
  • the chemical processes needed are devised in such a way that they can handle the complexities of chemical components in the waste products.
  • Waste plastics are, on a general level, very heterogeneous materials. Depending on the polymer type and in what application it has been used, different plastic products will contain different types of additives such as pigments, fillers, flame retardants and so forth. When the waste plastic is converted into LWP via e.g. pyrolysis, the polymers and the various additives etc.
  • LWP low-density polyethylene
  • Conversion of LWP into higher quality value-added products entails the use of catalytic processes, and catalysts that are typically employed in such processes are sensitive to different impurities, i.e. the activity of the catalysts can be deactivated due to deposition of various catalyst poisons.
  • LWP contains various impurities that are detrimental to catalysts, and consequently its further catalytic processing is technically more challenging e.g. when compared to conventional crude oil. This has led to the present invention, where these problems have been resolved by the process steps as claimed. Claimed process allows the processing of waste plastics to be made continuous and economical without having to worry about the damage and detrimental effects caused to the assets carrying out those processing.
  • Figure 1 is a schematic view of a specific embodiment of the current invention.
  • the current invention relates to a method of processing liquefied waste plastic, wherein the method comprises a first hydrotreatment of the LWP in mild conditions followed by blending the hydrotreated LWP with a stream comprising hydrocarbons.
  • liquefied waste plastic is hereby meant a liquid product produced from any waste plastic through a non-oxidative thermolysis process.
  • liquefied waste plastic is produced by pyrolysis of waste plastic.
  • Other processes to produce LWP include but are not limited to hydrothermal liquefaction processes.
  • the LWP is a mixture of hydrocarbonaceous organic components with a wide range of carbon chain lengths. Provided the large variations of carbon chain lengths and chemical structures and the properties of the LWP varies depending on the types of plastics (polymers) used in the production of LWP, the type of liquefaction process and conditions of the liquefaction process.
  • Typical waste plastic feedstock used in the liquefaction method includes mainly polyethylene with varying amounts of polypropylene, polystyrene and other minor components such as polyamides, polyethylene terephthalate and polyvinyl chloride.
  • the liquefied waste plastic can be obtained by pyrolyzing waste plastic and subsequently collecting a liquid fraction from the pyrolyzed waste plastic.
  • the solid waste plastic is heated to a temperature of 400-600 °C under non-oxidative conditions.
  • the polymers thermally decompose and consequently release vapours and gases that exit the reactor in the gas phase.
  • This vapor/gas stream is subsequently cooled down to condense the LWP product and to separate the gases.
  • the LWP typically has a boiling range of about 40 °C - 550 °C, which corresponds approximately to carbon chain lengths of C5 to C55. Depending on the conversion technology, the final boiling point of the LWP can go up to 750 °C.
  • LWP is a thermal cracking product of various polymers and is a complex mixture of mainly paraffins, olefins, naphthenes and aromatic hydrocarbons.
  • the total amount of olefins is typically high, from 40 wt.% to 60 wt.%, whereas the amount of aromatic hydrocarbons is typically lower than 20 wt.%.
  • LWP also contains heteroatoms, including oxygen, nitrogen, chlorine and sulphur, in the form of organic compounds with heteroatom substituents. The amounts of heteroatoms vary depending on the polymers used in production of LWP. Water is usually removed from the LWP product, but some dissolved water may still be present in the LWP.
  • the liquefied waste plastic can also undergo pre-treatment processes before the hydrotreatments according to the present invention.
  • the LWP undergoes a pre-treatment step before hydrotreatment step a) and the pre-treatment step comprises reactive extraction, solvent extraction, adsorption, filtration, centrifugation, oxidation, reduction or any combination thereof.
  • the catalyst may, for example, comprise at least one component selected from IUPAC group 6, 8 or 10 of the Periodic Table of Elements.
  • the catalyst preferably contains Mo and at least one further transition metal on a support. Examples of such a supported catalyst are a supported NiMo catalyst or a supported CoMo catalyst, or a mixture of both.
  • the support preferably comprises alumina and/or silica. These catalysts are usually employed as sulphided catalysts to ensure that the catalysts are in their active (sulphided) form. Turning the catalysts into their active (sulphided) form may be achieved by sulphiding them in advance (i.e.
  • the hydrotreating employs a catalyst and the catalyst is a supported NiMo catalyst and the support comprises alumina (NiMo/Al 2 O 3 ) and/or the catalyst is a supported CoMo catalyst and the support comprises alumina (CoMo/Al 2 O 3 ).
  • the catalyst of the hydrotreatment step a) is preferably supported NiMo, wherein the support preferably comprises alumina and/or silica.
  • the hydrotreatment step a) is repeated before the subsequent blending step.
  • the hydrotreatment step a) can be repeated to ensure sufficient hydrotreatment of LWP in the stream.
  • the possible need for repeating the hydrotreatment step a) depends on among others, on the hydrotreatment conditions, the hydrotreatment catalyst and reactor design, such as number of reactors, type of catalyst beds and number of catalyst beds in the reactors and so forth.
  • the stream of LWP consists only of LWP and the hydrotreatment in step a) is performed only on LWP.
  • the hydrotreatment a) in mild hydrotreatment conditions is performed solely on a stream containing only LWP and no other streams are directed to the first hydrotreatment step (step a) in claims).
  • the hydrotreatment step a) in this embodiment is a step where only components of the stream of LWP originating from waste plastic are hydrotreated in the mild hydrotreatment conditions.
  • the hydrotreatment step a) includes a step where a part of the formed stream of hydrotreated LWP from the hydrotreatment step a) is recycled back to the reactor carrying out the hydrotreatment step a).
  • the amount of recycling depends among others on the hydrotreatment conditions, the hydrotreatment catalyst and reactor design, such as number of reactors, type of catalyst bed and number of catalyst beds in the reactors.
  • a stream of first hydrotreated LWP is formed.
  • the formed hydrotreated LWP stream contains lower amounts of impurities, contaminants and harmful components compared to the before hydrotreated LWP feed.
  • impurities, contaminants and harmful components is herein meant any substance, compound or composition which have detrimental properties to any component, equipment or catalyst downstream of the hydrotreatment.
  • Especially harmful components are compounds containing hetero atoms, metals and metalloids.
  • Especially harmful hetero atoms include halogens such as chlorine.
  • Especially harmful metals include but are not limited to mercury, lead, sodium, arsenic, vanadium, iron, zinc and aluminium.
  • conjugated diolefins and olefins are considered agents causing coking or fouling which have to be minimised from the LWP in order for the treated LWP to be used downstream as a feedstock for steam cracking for example.
  • the purpose of hydrotreating a stream of liquified waste plastic (LWP) according to the invention is to reduce the risk of harmful and/or detrimental properties of any of the impurities, contaminants and harmful components, which might be present in the LWP.
  • the hydrotreating step reduces the amount of these components and therefore reduces the risks and harms they would otherwise pose on any component, equipment or catalyst downstream of the hydrotreatment.
  • the conjugated diolefin content in the LWP is reduced to below 0.2 wt.%.
  • the method of the current invention further comprises blending the stream of hydrotreated LWP obtained from mild hydrotreatment step a), with a stream comprising hydrocarbons to form a mixed stream comprising hydrotreated LWP and hydrocarbons.
  • the stream comprising hydrocarbons would have a different impurities profile than the LWP feed being subjected to the hydrotreatment step a), since said hydrocarbons is of any origins other than LWP thus "hydrocarbons" and “hydrocarbons of other origins" are to mean synonymously.
  • hydrocarbons of other origins in the form of stream is selected from vacuum gas oil (VGO) fraction, gas oil (GO) fraction, heavy gas oil (HGO) fraction, kerosene fraction, light gas oil fraction, atmospheric residue (AR) fraction, vacuum residue (VR) fraction and deasphalted oil (DAO) fraction.
  • VGO vacuum gas oil
  • GO gas oil
  • HGO heavy gas oil
  • kerosene fraction light gas oil fraction
  • AR atmospheric residue
  • VR vacuum residue
  • DAO deasphalted oil
  • the other suitable hydrocarbon streams to be used for blending include a crude oil-derived feedstock comprising at least one crude oil-fraction, or a bio-based fats or oils or fatty acids, or lignocellulosic based hydrocarbons, or Fischer Tropsch or other synthetic hydrocarbons.
  • the stream of hydrocarbons to be blended with the hydrotreated LWP will typically have a higher temperature compared to the stream of hydrotreated LWP.
  • the mixed stream of hydrotreated LWP and hydrocarbons contains up to 70 wt.% LWP based on total weight of stream, preferably the content of LWP in said stream is from 5 wt.% to 70 wt.%, more preferably from 10 wt.% to 50 wt.% and even more preferably from 15 wt.% to 30 wt.%.
  • the method further comprises c) hydrotreating said mixed stream of hydrotreated LWP and hydrocarbons in the presence of hydrogen and a catalyst in severe hydrotreatment conditions to provide a refined stream.
  • the hydrotreatment step c) is defined by its severe conditions which is carried out at a temperature of 355 °C to 400 °C, preferably 360°C to 390°C
  • hydrotreatment step c) is referred to as the hydrotreatment step subsequent to hydrotreatment step a) after the hydrotreated stream of step a) has been blended with a stream of hydrocarbons of other origins.
  • the catalyst of the hydrotreatment step a) and c) is a supported catalyst, and the catalyst preferably comprises at least one component selected from IUPAC group 6, 8 or 10 of the Periodic Table of Elements.
  • the supported catalyst can contain Mo and at least one further transition metal on a support, such as a supported NiMo catalyst or a supported CoMo catalyst, wherein the support preferably comprises alumina and/or silica.
  • the catalyst is a supported CoMo catalyst and the support comprises alumina (CoMo/Al 2 O 3 ) and/or the catalyst is a supported NiMo catalyst and the support comprises alumina (NiMo/Al 2 O 3 ).
  • the conditions of the hydrotreatment step c) are preferably selected from the following:
  • hydrotreatment steps a) and c) can be carried out respectively in a single reactor unit comprising at least one catalyst bed.
  • hydrotreatment step a) and c) can be carried out respectively in a reactor system comprising at least two reactor units, wherein each reactor unit contains at least one catalyst bed.
  • hydrogen is being mixed with the LWP before carrying out hydrotreatment step a) and/or step c).
  • the LWP undergoes a pre-treatment step before hydrotreatment step a) and the pre-treatment step comprises reactive extraction, solvent extraction, adsorption, filtration, centrifugation, oxidation, reduction or any combination thereof.
  • the method further comprises a step of adding water to said process and/or removal of an aqueous phase from said process after said hydrotreatment step a) and/or after said hydrotreatment c).
  • water is added to the process after any of the hydrotreatment steps in order to remove impurities.
  • the impurities are or become water soluble in the hydrotreatment and can thus be removed by washing the hydrotreated LWP stream with water.
  • the water soluble impurities are dissolved in the water stream and the aqueous phase containing the impurities is then decanted from the hydrotreated LWP stream.
  • the method further comprises a step of subjecting the refined stream after the hydrotreatment step c), to one or more fractionation step(s) to form two or more product streams.
  • the fractionated product streams include a naphtha fraction having a 5-95 wt.% boiling point range of 30-200 °C, preferably from about 30 °C to about 180 °C, more preferably from about 30 °C to about 110 °C, and a middle distillate fraction having a 5-95 wt.% having a boiling point from about 150 °C to about 400 °C, preferably from about 160 °C to about 360 °C, and more preferably from about 160 °C to about 330 °C, and a liquefied petroleum gas (LPG) fraction comprising one or more of ethane, propane or butane.
  • the naphtha fraction can further be subjected to steam cracking, and/or the middle distillate can further be subjected to steam cracking, and/or the LPG fraction can
  • hydrotreatment step a) and hydrotreatment step c) are carried out in a reactor system comprising one or more reactors, each reactor having one or more catalyst beds and at least one reactor with a direct hydrogen feed to the reactor.
  • the reactor designated for the hydrotreatment step a) and c) can also be carried out respectively in separate reactors, each having a plurality of independent catalyst beds and independent reaction temperatures, or any combination thereof.
  • a LWP product, P1 obtainable by hydrotreating LWP according to hydrotreatment step a) and blending according to step b) and wherein the product comprises
  • ICP-MS/MS Metals measurement by ICP-MS/MS is performed on a sample that is warmed to liquid if needed prior to weighing. It is digested with acids in the microwave oven to a clear water/acid matrix, diluted to a known amount and analysed against the acid based calibration using ICP-MS/MS. Low elemental results are determined as ppb ( ⁇ g/kg).
  • the method further comprises a step of subjecting the refined stream after the hydrotreatment step a), and blending step b), i.e., product P1, to one or more fractionation step(s) to form two or more product streams.
  • the fractionated product streams include a naphtha fraction having a 5-95 wt.% boiling point range of 30-200 °C, preferably from about 30 °C to about 180 °C, more preferably from about 30 °C to about 110 °C, and a middle distillate fraction having a 5-95 wt.% having a boiling point from about 150 °C to about 400 °C, preferably from about 160 °C to about 360 °C, and more preferably from about 160 °C to about 330 °C, and a liquefied petroleum gas (LPG) fraction comprising one or more of ethane, propane or butane.
  • LPG liquefied petroleum gas

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (18)

  1. Verfahren zur Verarbeitung von verflüssigten Kunststoffabfällen (Liquefied Waste Plastic - LWP), wobei das Verfahren umfasst:
    Schritt a) Wasserstoffbehandlung (Hydrotreating) eines Stroms von verflüssigten Kunststoffabfällen (LWP) bei Vorhandensein von Wasserstoff und eines Katalysators in einem ersten Wasserstoffbehandlungsschritt unter milden Wasserstoffbehandlungsbedingungen bei einer Temperatur von 170 °C bis 350 °C, um einen Strom von wasserstoffbehandelten LWP zu bilden, in einem Reaktorsystem, das mindestens einen Reaktor umfasst, der jeweils mindestens ein Katalysatorbett umfasst,
    Schritt b) Mischen des Stroms von wasserstoffbehandelten LWP mit einem Strom, der Kohlenwasserstoffe umfasst, um einen gemischten Strom von wasserstoffbehandelten LWP und Kohlenwasserstoffen zu bilden, wobei der gemischte Strom, der wasserstoffbehandelte LWP und Kohlenwasserstoffe umfasst, auf einer Temperatur von 140 °C bis 350 °C gehalten wird, bevor er dem Wasserstoffbehandlungsschritt c) unterzogen wird, und
    Schritt c) Wasserstoffbehandeln des gemischten Stroms von wasserstoffbehandelten LWP und Kohlenwasserstoffen bei Vorhandensein von Wasserstoff und eines Katalysators unter rauen Wasserstoffbehandlungsbedingungen bei einer Temperatur von 355 °C bis 400 °C, um einen raffinierten Strom bereitzustellen.
  2. Verfahren nach Anspruch 1, wobei der Strom von LWP vor dem Wasserstoffbehandlungsschritt a) einem Vorbehandlungsschritt unterzogen wird und der Vorbehandlungsschritt Reaktivextraktion, Solventextraktion, Adsorption, Filtration, Zentrifugieren, Oxidation, Reduktion oder eine beliebige Kombination davon umfasst.
  3. Verfahren nach einem der vorhergehenden Ansprüche, wobei der Strom, der Kohlenwasserstoffe umfasst, ein aus Rohöl gewonnener Einsatzstoff ist, der mindestens eine Rohölfraktion oder biobasierte Fette oder Öle oder Fettsäuren oder Kohlenwasserstoffe auf Lignocellulosebasis oder Fischer-Tropsch-Kohlenwasserstoffe umfasst, wobei die Rohölfraktion ausgewählt wird aus Vakuumgasöl(VGO)-Fraktion, Gasöl(GO)-Fraktion, schwerer Gasöl(HGO)-Fraktion, Kerosinfraktion, leichter Gasölfraktion, atmosphärischer Rückstand(AR)-Fraktion, Vakuumrückstand(VR)-Fraktion und entasphaltierter Öl(DAO)-Fraktion.
  4. Verfahren nach einem der vorhergehenden Ansprüche, wobei der gemischte Strom von wasserstoffbehandelten LWP und Kohlenwasserstoffen bis zu 70 Gew.-% LWP, bezogen auf das Gesamtgewicht des Stroms, umfasst, wobei der Gehalt an LWP in dem Strom vorzugsweise zwischen 5 Gew.-% und 70 Gew.-%, mehr zu bevorzugen zwischen 10 Gew.-% und 50 Gew.-% und sogar noch mehr zu bevorzugen zwischen 15 Gew.-% und 30 Gew.-%, beträgt.
  5. Verfahren nach einem der vorhergehenden Ansprüche, wobei der Katalysator in dem Wasserstoffbehandlungsschritt a) ein Trägerkatalysator ist und der Katalysator vorzugsweise mindestens eine Komponente umfasst, die ausgewählt ist aus der IUPAC-Gruppe 6, 8 oder 10 des Periodensystems der Elemente.
  6. Verfahren nach Anspruch 5, wobei der Trägerkatalysator Mo und mindestens ein weiteres Übergangsmetall auf einem Träger umfasst, wie beispielsweise einen NiMo-Trägerkatalysator oder einen CoMo-Trägerkatalysator, wobei der Träger vorzugsweise Aluminiumoxid und/oder Siliziumdioxid umfasst.
  7. Verfahren nach Anspruch 6, wobei der Katalysator ein CoMo-Trägerkatalysator ist und der Träger Aluminiumoxid (CoMo/Al2O3) umfasst und/oder der Katalysator ein NiMo-Trägerkatalysator ist und der Träger Aluminiumoxid (NiMo/Al2O3) umfasst.
  8. Verfahren nach einem der vorhergehenden Ansprüche, wobei das Verfahren ferner nach dem Wasserstoffbehandlungsschritt a) und/oder nach dem Wasserstoffbehandlungsschritt c) einen Schritt des Beimengens von Wasser zu dem Prozess und/oder des Beseitigens einer wässrigen Phase von dem Prozess umfasst.
  9. Verfahren nach einem der vorhergehenden Ansprüche, wobei der Wasserstoffbehandlungsschritt a) vor dem Schritt des Mischens des Stroms von wasserstoffbehandelten LWP mit einem Strom, der Kohlenwasserstoffe umfasst, wiederholt wird, um einen gemischten Strom von wasserstoffbehandelten LWP und Kohlenwasserstoffen zu erhalten.
  10. Verfahren nach einem der vorhergehenden Ansprüche, wobei der Strom von LWP lediglich aus LWP besteht und der Wasserstoffbehandlungsschritt a) lediglich auf LWP durchgeführt wird.
  11. Verfahren nach einem der vorhergehenden Ansprüche, wobei der Wasserstoffbehandlungsschritt a) unter den folgenden Bedingungen durchgeführt wird
    - ein Verhältnis von H2 zu Öl beträgt 200 bis 450 Nm3/stdm3, vorzugsweise 220 bis 400 Nm3/stdm3;
    - einer LHSV von 0,1 bis 2,0 h-1, vorzugsweise 0,2 bis 0,5 h-1;
    - einer Temperatur von 170 bis 340 °C.
  12. Verfahren nach einem der Ansprüche 1 bis 11, wobei der Wasserstoffbehandlungsschritt c) unter den folgenden Bedingungen durchgeführt wird
    - ein Verhältnis von H2 zu Öl beträgt 150 bis 400 Nm3/stdm3, vorzugsweise 180 bis 250 Nm3/stdm3;
    - einer LHSV von 0,5 bis 2,0 h-1, vorzugsweise 1,0 bis 1,5 h-1;
    - einer Temperatur von 355 bis 400 °C, vorzugsweise 360 bis 390 °C.
  13. Verfahren nach einem der Ansprüche 1 bis 12, wobei das Verfahren ferner einen Schritt des Aussetzens des raffinierten Stroms gegenüber einem oder mehreren Fraktionierungsschritt/en umfasst, um zwei oder mehr Produktströme zu bilden, wobei die Produktströme vorzugsweise eine Naphtha-Fraktion, die einen 5 bis 95 Gew.-% Siedepunktbereich von 30 bis 200 °C, vorzugsweise von etwa 30 °C bis etwa 180 °C, mehr zu bevorzugen von etwa 30 °C bis etwa 110 °C, aufweist, und eine Mitteldestillatfraktion, die einen 5 bis 95 Gew.-% Siedepunkt von etwa 150 °C bis etwa 400 °C, vorzugsweise von etwa 160 °C bis etwa 360 °C, und mehr zu bevorzugen von etwa 160 °C bis etwa 330 °C, aufweist, umfassen.
  14. Verfahren nach Anspruch 13, wobei die Naphtha-Fraktion ferner Steamcracking unterzogen wird und/oder das Mitteldestillat ferner Steamcracking unterzogen wird und/oder die LPG-Fraktion ferner Steamcracking unterzogen wird.
  15. Verfahren nach einem der Ansprüche 1 bis 14, wobei die Wasserstoffbehandlungsschritte a) und c) jeweils in einer Einzelreaktoreinheit durchgeführt werden, die mindestens ein Katalysatorbett umfasst, oder die Wasserstoffbehandlungsschritte a) und c) jeweils in einem Reaktorsystem, das mindestens zwei Reaktoreinheiten umfasst, wobei jede Reaktoreinheit mindestens ein Katalysatorbett umfasst, oder einer beliebigen Kombination davon durchgeführt werden.
  16. Verfahren nach einem der vorhergehenden Ansprüche, wobei der mindestens eine Reaktor eine direkte Wasserstoffabschreckung zum Reaktor aufweist.
  17. Verfahren nach einem der Ansprüche 1 bis 16, wobei vor dem Durchführen des Wasserstoffbehandlungsschritts a) und Schritts c) Wasserstoff mit dem Strom von LWP gemischt wird.
  18. Gereinigtes Kohlenwasserstoffprodukt, das durch Wasserstoffbehandeln von LWP gemäß dem Wasserstoffbehandlungsschritt a) und Mischen gemäß dem Schritt b) nach Anspruch 1 erhältlich ist, wobei das Produkt umfasst
    - eine verringerte Menge an Silizium, um, gemessen durch ICP-MS/MS, unter 6 mg/kg, mehr zu bevorzugen < 1 mg/kg, zu betragen, und/oder Phosphor, um unter 5 mg/kg, vorzugsweise 1 mg/kg, zu betragen,
    - ein niedriges Verhältnis von Diolefin zum Gesamtolefingehalt, um, gemessen durch ASTMD8071, unter 0,01, mehr zu bevorzugen unter 0,001, zu betragen,
    - ein niedriges Verhältnis von konjugiertem Diolefin zu nicht konjugiertem Diolefin, um, gemessen durch ASTMD8071, unter 2, mehr zu bevorzugen unter 1, zu betragen
    - einen Halogengehalt von unter 5 mg/kg, vorzugsweise 1 mg/kg.
EP21205587.5A 2021-10-29 2021-10-29 Verfahren zur behandlung von kunststoffabfällen Active EP4174150B1 (de)

Priority Applications (12)

Application Number Priority Date Filing Date Title
EP21205587.5A EP4174150B1 (de) 2021-10-29 2021-10-29 Verfahren zur behandlung von kunststoffabfällen
ES21205587T ES2992534T3 (es) 2021-10-29 2021-10-29 Método de tratamiento de residuos plásticos
DK21205587.5T DK4174150T3 (da) 2021-10-29 2021-10-29 Fremgangsmåde til behandling af plastaffald
FIEP21205587.5T FI4174150T3 (fi) 2021-10-29 2021-10-29 Menetelmä jätemuovin käsittelemiseksi
HUE21205587A HUE069562T2 (hu) 2021-10-29 2021-10-29 Eljárás mûanyaghulladék kezelésére
PL21205587.5T PL4174150T3 (pl) 2021-10-29 2021-10-29 Sposób obróbki odpadów z tworzyw sztucznych
CA3235790A CA3235790A1 (en) 2021-10-29 2022-10-28 Method of treating waste plastic
US18/705,766 US20250002798A1 (en) 2021-10-29 2022-10-28 Method of treating waste plastic
PCT/EP2022/080245 WO2023073194A1 (en) 2021-10-29 2022-10-28 Method of treating waste plastic
KR1020247015111A KR20240073975A (ko) 2021-10-29 2022-10-28 폐플라스틱의 처리 방법
MX2024004679A MX2024004679A (es) 2021-10-29 2022-10-28 Metodo de tratamiento de residuos de plastico.
JP2024525487A JP2024541709A (ja) 2021-10-29 2022-10-28 廃プラスチックを処理するための方法

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP21205587.5A EP4174150B1 (de) 2021-10-29 2021-10-29 Verfahren zur behandlung von kunststoffabfällen

Publications (2)

Publication Number Publication Date
EP4174150A1 EP4174150A1 (de) 2023-05-03
EP4174150B1 true EP4174150B1 (de) 2024-09-25

Family

ID=78414522

Family Applications (1)

Application Number Title Priority Date Filing Date
EP21205587.5A Active EP4174150B1 (de) 2021-10-29 2021-10-29 Verfahren zur behandlung von kunststoffabfällen

Country Status (6)

Country Link
EP (1) EP4174150B1 (de)
DK (1) DK4174150T3 (de)
ES (1) ES2992534T3 (de)
FI (1) FI4174150T3 (de)
HU (1) HUE069562T2 (de)
PL (1) PL4174150T3 (de)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI20235610A1 (en) * 2023-05-31 2024-12-01 Neste Oyj Processing of liquid plastic waste
WO2025219653A1 (en) 2024-04-19 2025-10-23 Neste Oyj Liquid phase hydrotreatment of liquefied waste plastic

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH1161148A (ja) 1997-08-21 1999-03-05 Jgc Corp 廃プラスチックの処理方法
US20090253948A1 (en) 2008-04-06 2009-10-08 Mccall Michael J Fuel and Fuel Blending Components from Biomass Derived Pyrolysis Oil
WO2014001633A1 (en) 2012-06-25 2014-01-03 Upm-Kymmene Corporation Process for producing hydrocarbons
US20140275666A1 (en) 2013-03-14 2014-09-18 Kior, Inc. Two stage process for producing renewable biofuels
WO2020254629A1 (en) 2019-06-20 2020-12-24 Haldor Topsøe A/S Process for pre-heating hydrotreatment reactor feed stream
WO2021105326A1 (en) 2019-11-29 2021-06-03 Neste Oyj Two-step process for converting liquefied waste plastics into steam cracker feed
WO2021110395A1 (fr) 2019-12-02 2021-06-10 IFP Energies Nouvelles Procede de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation dans une unite de vapocraquage
WO2021165178A1 (fr) 2020-02-21 2021-08-26 IFP Energies Nouvelles Procede optimise de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation
WO2021204817A1 (en) 2020-04-07 2021-10-14 Total Research & Technology Feluy Purification of waste plastic based oil via a two steps hydrotreatment
WO2022023262A1 (fr) 2020-07-30 2022-02-03 IFP Energies Nouvelles Procede de traitement d'huiles de pyrolyse de plastiques incluant un hydrocraquage en une etape

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH1161148A (ja) 1997-08-21 1999-03-05 Jgc Corp 廃プラスチックの処理方法
US20090253948A1 (en) 2008-04-06 2009-10-08 Mccall Michael J Fuel and Fuel Blending Components from Biomass Derived Pyrolysis Oil
WO2014001633A1 (en) 2012-06-25 2014-01-03 Upm-Kymmene Corporation Process for producing hydrocarbons
US20140275666A1 (en) 2013-03-14 2014-09-18 Kior, Inc. Two stage process for producing renewable biofuels
WO2020254629A1 (en) 2019-06-20 2020-12-24 Haldor Topsøe A/S Process for pre-heating hydrotreatment reactor feed stream
WO2021105326A1 (en) 2019-11-29 2021-06-03 Neste Oyj Two-step process for converting liquefied waste plastics into steam cracker feed
WO2021110395A1 (fr) 2019-12-02 2021-06-10 IFP Energies Nouvelles Procede de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation dans une unite de vapocraquage
WO2021165178A1 (fr) 2020-02-21 2021-08-26 IFP Energies Nouvelles Procede optimise de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation
WO2021204817A1 (en) 2020-04-07 2021-10-14 Total Research & Technology Feluy Purification of waste plastic based oil via a two steps hydrotreatment
WO2021204819A1 (en) 2020-04-07 2021-10-14 Total Research & Technology Feluy Purification of waste plastic based oil with a first trap and a first hydrotreatment and a second trap and a second hydrotreatment
WO2022023262A1 (fr) 2020-07-30 2022-02-03 IFP Energies Nouvelles Procede de traitement d'huiles de pyrolyse de plastiques incluant un hydrocraquage en une etape

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
ANONYMOUS: "ASTM D8071-21 Standard Test Method for Determination of Hydrocarbon Group Types and Select Hydrocarbon and Oxygenate Compounds in Automotive Spark-Ignition Engine Fuel Using Gas Chromatography with Vacuum Ultraviolet Absorption Spectroscopy Detection (GC-VUV)", ASTM NORM, ASTM INTERNATIONAL, 1 August 2021 (2021-08-01), pages 1 - 18, XP093291467, DOI: 10.1520/D8071-21

Also Published As

Publication number Publication date
PL4174150T3 (pl) 2025-03-03
FI4174150T3 (fi) 2024-11-28
ES2992534T3 (es) 2024-12-13
DK4174150T3 (da) 2024-11-11
HUE069562T2 (hu) 2025-03-28
EP4174150A1 (de) 2023-05-03

Similar Documents

Publication Publication Date Title
KR102420209B1 (ko) 중질 연료유의 화학제품으로의 전환
CN115232639B (zh) 用于原油转化的系统和方法
CA3197588A1 (en) Co-processing of polymer waste-based material for jet fuel production
KR100293752B1 (ko) 폐물또는폐플라스틱재료를처리하기위한방법
KR20160146676A (ko) 혼합 폐 플라스틱 (mwp)을 가치있는 석유화학제품으로 전환하는 방법
EP4174150B1 (de) Verfahren zur behandlung von kunststoffabfällen
CA3227116A1 (en) Method of treating waste plastic
CA3236234A1 (en) A process for hydrotreatment of aromatic nitrogen compounds
WO2024246419A1 (en) Upgrading liquefied waste plastics
WO2022144490A1 (en) Method for processing liquefied waste polymers
FI130219B (en) METHOD FOR HANDLING WASTE PLASTIC
US20250002798A1 (en) Method of treating waste plastic
KR20240088886A (ko) 열분해 오일로부터 저-방향족 탄화수소의 제조 과정
US20250382531A1 (en) A process for stabilization of an unstable raw hydrocarbonaceous product
KR20240155760A (ko) 폐플라스틱으로부터 정제 탄화수소의 제조 방법 및 제조 시스템
WO2024121460A1 (en) Marine fuel product
CN118922515A (zh) 用于生产运输燃料的方法
WO2025219653A1 (en) Liquid phase hydrotreatment of liquefied waste plastic
WO2025219654A1 (en) Next generation liquefied waste plastic upgrading
CN105722955A (zh) 加氢处理方法以及与多功能加氢处理器相关的应用

Legal Events

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

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN PUBLISHED

AK Designated contracting states

Kind code of ref document: A1

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

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20231103

RBV Designated contracting states (corrected)

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

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20240422

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

P01 Opt-out of the competence of the unified patent court (upc) registered

Free format text: CASE NUMBER: APP_41781/2024

Effective date: 20240716

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

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

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602021019236

Country of ref document: DE

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

Effective date: 20241106

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: FI

Ref legal event code: FGE

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2992534

Country of ref document: ES

Kind code of ref document: T3

Effective date: 20241213

REG Reference to a national code

Ref country code: SK

Ref legal event code: T3

Ref document number: E 45310

Country of ref document: SK

REG Reference to a national code

Ref country code: SE

Ref legal event code: TRGR

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG9D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20241226

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20241225

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20241104

Year of fee payment: 4

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20241225

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20241226

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: TR

Payment date: 20241106

Year of fee payment: 4

REG Reference to a national code

Ref country code: HU

Ref legal event code: AG4A

Ref document number: E069562

Country of ref document: HU

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20250127

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20250125

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: DE

Ref legal event code: R026

Ref document number: 602021019236

Country of ref document: DE

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925

PLAX Notice of opposition and request to file observation + time limit sent

Free format text: ORIGINAL CODE: EPIDOSNOBS2

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20241029

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20241031

26 Opposition filed

Opponent name: TOPSOE A/S

Effective date: 20250623

Opponent name: KRAUS & LEDERER PARTGMBB

Effective date: 20250623

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: PL

Payment date: 20250912

Year of fee payment: 5

Ref country code: NL

Payment date: 20250912

Year of fee payment: 5

Ref country code: IT

Payment date: 20250922

Year of fee payment: 5

REG Reference to a national code

Ref country code: AT

Ref legal event code: UEP

Ref document number: 1726643

Country of ref document: AT

Kind code of ref document: T

Effective date: 20240925

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BG

Payment date: 20250916

Year of fee payment: 5

Ref country code: BE

Payment date: 20250917

Year of fee payment: 5

Ref country code: GB

Payment date: 20250904

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20250908

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20250910

Year of fee payment: 5

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20241029

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CZ

Payment date: 20250929

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SK

Payment date: 20250912

Year of fee payment: 5

PLAF Information modified related to communication of a notice of opposition and request to file observations + time limit

Free format text: ORIGINAL CODE: EPIDOSCOBS2

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: HU

Payment date: 20250929

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20250902

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NO

Payment date: 20251009

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 20260113

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FI

Payment date: 20251014

Year of fee payment: 5

Ref country code: DK

Payment date: 20251014

Year of fee payment: 5

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20240925