WO2024121460A1 - Marine fuel product - Google Patents
Marine fuel product Download PDFInfo
- Publication number
- WO2024121460A1 WO2024121460A1 PCT/FI2023/050670 FI2023050670W WO2024121460A1 WO 2024121460 A1 WO2024121460 A1 WO 2024121460A1 FI 2023050670 W FI2023050670 W FI 2023050670W WO 2024121460 A1 WO2024121460 A1 WO 2024121460A1
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- WO
- WIPO (PCT)
- Prior art keywords
- marine fuel
- fuel product
- fraction boiling
- feed
- fraction
- Prior art date
Links
- 239000000295 fuel oil Substances 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 claims abstract description 61
- 230000008569 process Effects 0.000 claims abstract description 49
- 239000004033 plastic Substances 0.000 claims abstract description 36
- 229920003023 plastic Polymers 0.000 claims abstract description 36
- 239000002699 waste material Substances 0.000 claims abstract description 36
- 239000010779 crude oil Substances 0.000 claims abstract description 15
- 238000005194 fractionation Methods 0.000 claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 claims abstract description 8
- 238000009835 boiling Methods 0.000 claims description 56
- 239000003054 catalyst Substances 0.000 claims description 22
- 239000003921 oil Substances 0.000 claims description 22
- 239000000203 mixture Substances 0.000 claims description 18
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 11
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 8
- 230000000737 periodic effect Effects 0.000 claims description 4
- 239000003350 kerosene Substances 0.000 claims description 3
- 239000000047 product Substances 0.000 description 40
- 235000019198 oils Nutrition 0.000 description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 15
- 239000000446 fuel Substances 0.000 description 14
- 229910052799 carbon Inorganic materials 0.000 description 13
- 238000010438 heat treatment Methods 0.000 description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 11
- 239000011593 sulfur Substances 0.000 description 11
- 229910052717 sulfur Inorganic materials 0.000 description 11
- 239000007789 gas Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 8
- 238000012545 processing Methods 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000003925 fat Substances 0.000 description 6
- 235000019197 fats Nutrition 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 229920000642 polymer Polymers 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 229910003294 NiMo Inorganic materials 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 125000005842 heteroatom Chemical group 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- -1 polyethylene Polymers 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- CPRMKOQKXYSDML-UHFFFAOYSA-M rubidium hydroxide Chemical compound [OH-].[Rb+] CPRMKOQKXYSDML-UHFFFAOYSA-M 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- 235000019737 Animal fat Nutrition 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 101150063042 NR0B1 gene Proteins 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 229910001860 alkaline earth metal hydroxide Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000012620 biological material Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000019688 fish Nutrition 0.000 description 1
- 235000021323 fish oil Nutrition 0.000 description 1
- 229940013317 fish oils Drugs 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 229910052945 inorganic sulfide Inorganic materials 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 235000012254 magnesium hydroxide Nutrition 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 239000010773 plant oil Substances 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 239000005020 polyethylene terephthalate Substances 0.000 description 1
- 229920000139 polyethylene terephthalate Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- UUCCCPNEFXQJEL-UHFFFAOYSA-L strontium dihydroxide Chemical compound [OH-].[OH-].[Sr+2] UUCCCPNEFXQJEL-UHFFFAOYSA-L 0.000 description 1
- 229910001866 strontium hydroxide Inorganic materials 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000001149 thermolysis Methods 0.000 description 1
- 235000015112 vegetable and seed oil Nutrition 0.000 description 1
- 239000008158 vegetable oil Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
-
- 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
-
- 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
-
- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/22—Separation of effluents
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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
Herein is described a marine fuel product obtainable by hydrotreating a feed comprising liquefied waste plastic (LWP) and a crude oil component, wherein the hydrotreating is a hydrotreatment process followed by fractionation to obtain the marine fuel product as a fraction. Also, described is a marine fuel and a method for producing marine fuel. Described is also a use of liquefied waste plastic in a feed for a process for producing marine fuel.
Description
MARINE FUEL PRODUCT
FIELD OF THE INVENTION
The present invention relates to a marine fuel product produced using a feed comprising liquefied waste plastic (LWP). The feed comprising LWP is subjected to a co-processing manner together with a crude oil component to a process to produce marine fuel product, wherein the process comprises hydrotreatment and fractionation. A novel marine fuel or marine fuel component is hereby described, which comprises hydrotreated LWP.
BACKGROUND OF THE INVENTION
According to the International Maritime Organisation (IMO) strategy, by 2050, global shipping should reduce greenhouse gas (GHG) emissions by at least 50 % compared to the 2008 levels. This puts a great challenge not only on energy efficiency of ship engines but also on developing alternative fuel solutions with the use of waste materials for maritime purposes. Using waste and circular materials also in fuel applications is sensible from an environmental and circular economy viewpoint and can also decrease the life-cycle carbon emissions.
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 and electricity would be collected.
There is a growing interest in making use of waste plastic for producing various hydrocarbon components, such as mixtures of hydrocarbons that can be used raw material for new plastics, chemicals and other materials and/or as liquid fuels. Similarly to fuels, direct incineration of waste plastic also produces energy, which can be captured and used for heating and/or production of electricity. However, in contrast to heat and electricity liquid fuels are excellent for storing energy, which can be transported and released when needed.
Plastics or polymers mainly constitute carbon and hydrogen. However, waste plastics also contain many heteroatom impurities, such as oxygen, nitrogen, metal and/or chlorine impurities. To enable production of high-quality hydrocarbon products waste plastics are treated by a liquefaction process, such as pyrolysis to produce liquefied waste plastic (LWP). Hydrocarbons, which can be used in
various applications such as fuel applications, can be produced from LWP using oil refinery processes.
Recent developments of marine fuels have mainly concerned reduction of sulfur content of the fuel. Although sulfur content is important from an environmental aspect there is also a need to develop more sustainable marine fuels with lowered life-cycle carbon emissions.
BRIEF DESCRIPTION OF THE INVENTION
An object of the present invention is thus to provide a marine fuel product with lower carbon emission compared to using only virgin crude oil. The present invention provides a marine fuel product obtainable using a feed comprising liquefied waste plastics. The marine fuel product is produced in a hydrotreating coprocess and a marine fuel product with improved fuel properties as well as lower carbon emissions can be obtained.
An object of the current invention is therefore to provide a marine fuel product obtainable by hydrotreating a feed comprising liquefied waste plastic (LWP) and a crude oil component, wherein the hydrotreating is a hydrotreatment process followed by fractionation to obtain the marine fuel product as a fraction.
A further object of the current invention is to provide a marine fuel and a method for producing marine fuel. A still further object of the invention is to provide a use of liquefied waste plastic as a feed for a process for producing marine fuel.
An advantage of the current invention is to enable upgrading of waste plastics to valuable products while at the same time obtaining marine fuel solutions with excellent fuel properties and lower carbon emissions. The current solution is easily adopted in existing refinery units and require very little or no modifications to existing facilities or equipment.
DETAILED DESCRIPTION OF THE INVENTION
The current invention relates to a novel marine fuel product, which is produced in a process where liquefied waste plastic (LWP) is used as one feedstock. The feed of the process is LWP and a crude oil component, which are upgraded in a hydrotreatment process. The hydrotreated product thus obtained is fractionated to obtain the marine fuel product. Surprisingly, LWP is found to be an excellent feed or part of a feed to obtain marine fuel with improved fuel properties. LWP is a recycled waste product and the carbon emission of the marine fuel produced from LWP is therefore lower compared to a feed of 100% virgin crude oil.
With the term "liquefied waste plastic", or LWP for short, is hereby meant a liquid product produced from any waste plastic through a liquefaction process. Liquefaction processes are typically non-oxidative thermolysis or thermal decomposition processes. Technologies include but are not limited to pyrolysis or hydrothermal liquefaction. 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 vary 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, polypropylene and/or polystyrene with varying amounts of other components such as polyamides, polyethylene terephthalate and polyvinyl chloride.
Liquefied waste plastic can be obtained by thermally decomposing waste plastic and subsequently collecting at least one liquid fraction from the process. In a typical pyrolysis process, 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 vapour/gas stream is subsequently cooled down to condense 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 C 5 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 sulfur, 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 have undergone pretreatment processes. LWP pretreatment processes include but are not limited to heat treatment, reactive extraction, solvent extraction, adsorption, filtration, centrifugation, oxidation, reduction or any combination thereof.
In one embodiment of the invention the process further comprises
pretreating the LWP, wherein the pretreatment is heat treatment in the presence of an alkaline substance in aqueous solution. The heat treatment involves subjecting the crude LWP feedstock to be in contact with an aqueous solution containing an amount of alkaline substance to form an admixture, and the admixture is then heated to at least 150°C. After heat treatment, the heat-treated admixture is then subjected to phase separation to obtain at least a pre-treated LWP material and an aqueous phase. The pre-treated LWP material obtained from the phase separation is then subjected to downstream processing such as hydrotreatment.
The heat treatment (HT) processing is preferably carried out at a temperature of 150°C or more, preferably 190°C or more, such as 200°C or more, 220°C or more, 240°C or more or 260°C or more. The HT processing is preferably carried out at a temperature of 450°C or less, preferably 400°C or less, 350°C or less, or 300°C or less. For example, the HT processing is carried out at a temperature in the range of 200°C to 350°C, preferably 220°C to 330°C, 240°C to 320°C, or 260°C to 300°C.
The alkaline substance contained in the aqueous solution is selected from the group consisting of alkali metal hydroxides and alkaline earth metal hydroxides, and preferably the basic substance is selected from the group consisting of KOH, NaOH, LiOH, Ca(OH)2, Mg(OH)2, RbOH, Sr(OH)2 and Ba(OH)2, preferably NaOH.
The target pH level of the aqueous solution in the HT process in the presence of alkaline substance is preferably 10.0 or more. With this minimum target pH level, good HT processing efficiency can be ensured. Although the HT processing efficiency is high as long as the target pH (and more preferably the actual pH of the aqueous phase) is 10.0 or more, even though there is no actual upper limit of the target pH. In view thereof, the target pH level (and preferably the actual pH level) is preferably in the range of from 10.0 to 14.0, such as 10.2 to 13.9, 10.3 to 13.8, 10.4 to 13.6, 10.5 to 13.5, 10.6 to 13.4, 10.7 to 13.3, 10.8 to 13.2, 10.9 to 13.1, or 11.0 to 13.0.
With the term "marine fuel" is here meant any hydrocarbonecous composition or mixture of hydrocarbons suitable as fuel for ships and other maritime vessels. Marine fuels are governed by the standard ISO 8217:2017 which specifies the requirement of hydrocarbons for use in marine diesel engines and boilers, but can also be used in stationary diesel engines of the same or similar types as those used for marine purposes. The standard ISO 8217 specifies the required density, viscosity, pour point flash point, sulfur content, cetane index and Calculated Carbon
Aromaticity Index (CCAI), among other required parameters.
All standards referred to herein are the latest revisions available at the filing date, unless otherwise mentioned.
The marine fuel product of the current invention is obtainable by hydrotreating a feed, as hereby defined, in a process that comprises hydrotreatment and fractionation. The process for obtaining the marine fuel products is a co-pro- cess, where liquefied waste plastic (LWP) is processed together with a crude oil component. The crude oil component can be any suitable mixture or stream of crude oil origin typically used in hydrotreatment and hydrodesulfurization processes, where especially marine fuel types of products are produced.
According to one embodiment of the invention the crude oil component is naphtha, kerosene, light gas oil (LGO), heavy gas oil (HGO), vacuum gas oil (VGO) or any mixture thereof. In one embodiment the feed and co-processing process can also comprise other components such as gas oil (GO) kerosene fraction, light gas oil fraction, atmospheric residue fraction, vacuum residue and deasphalted oil fraction, especially when also other fuel components besides marine fuel products are obtained in the hydrotreatment process.
The co-process hereby described can use a feed comprising LWP as a part of the total fraction. In one embodiment the amount of LWP in feed 5 wt.% to 40 wt.%, preferably 10 wt.% to 30 wt.% and more preferably 20 wt.% to 25 wt.%. Typically, the balance of the feed is HGO or VGO or a mixture thereof, but the feed can also contain other components. It has been found that already an amount of 10 wt.% LWP improves the marine fuel properties. At least an amount of 40 wt.%, or 20 wt.% can safely be used in the feed, without any detrimental effects to the products or process such as catalysts or equipment.
In one embodiment the feed further comprises biobased material. The biobased material can be any biological material such as vegetable oil, animal fat, fish fat, fish oil, algae oil, microbial oil, wood and/or other plant-based oil, fats contained in plants bred by means of gene manipulation, recycled waste and/or residue or combination thereof. Preferably the biobased material is selected from plant oil or fats, animal fats or oil, fish oils or fats, recycled fats from food industry and any combination thereof.
In one embodiment, the hydrotreating is a hydrodesulfurization (HDS) process. The hydrodesulfurization (HDS) process is any process which aims at reducing the sulfur amount in a feed using hydrogenation. A person skilled in the art is well familiar with various hydrodesulfurization processes used in oil refineries
and can adopt the current invention of a particular hydrodesulfurization process.
In one embodiment, the hydrodesulfurization process is performed in the presence of hydrogen and a hydrotreating catalyst. The hydrotreating catalyst can be a supported or unsupported catalyst comprising at least one component selected from 1UPAC group 6, 8 or 10 of the Periodic Table of Elements. In one embodiment the catalyst active site is Ni, Mo or Co catalyst. The support if present is preferably alumina and/or silica, preferably the support is AI2O3.
The supported hydrotreating catalyst is usually employed as sulfided catalyst to ensure that the catalyst is in its active (sulfided) form. Turning the catalyst into its active (sulfided) form may be achieved by sulfiding it in advance (i.e. before starting the hydrotreating reaction) and/or by adding sulfur containing feed (containing sulfur e.g. as an organic or inorganic sulfide). The feed may contain the sulfur from the start, or sulfur additives may be admixed to the feed.
In one embodiment, the supported catalyst is supported NiMo or C0M0 and the support comprises alumina. Preferred catalysts are NiMo/AhOs or C0M0/AI2O3, or a combination thereof.
The hydrodesulfurization conditions are typical for any oil refinery process and can be selected from the following conditions: a H2 to oil ratio is 150 - 400 Nm3/stdm3, preferably 180 - 250 Nm3/stdm3; a LHSV of 0.5 - 2.0 h 1, preferably 1.0 - 1.5 h 1; a temperature of 300-400 °C, preferably 350-390 °C, and a pressure of 4000-6000 kPa(a), preferably 4800-5500 kPa(a).
The current process also comprises fractionation of the hydrotreated product. A person skilled in the art is familiar with fractionation processes and many oil refinery processes include fractionation. Fractionations are typically performed by distillation, but also other fractionation techniques can be employed. In one embodiment the hydrotreated product is fractionated to obtain as marine fuel product a fraction boiling up to about 370 °C, preferably the fraction obtained as marine fuel product is a fraction boiling from about 300 °C up to about 370 °C.
Also, a fraction boiling above about 370 °C, especially above about 370 °C and up to about 600 °C is obtained. It has surprisingly been found that a fraction boiling up to about 370 °C and especially a fraction boiling from about 300 °C to about 370 °C fulfils the marine fuel requirements as set out in ISO 8217:2017 standard. Also, a fraction boiling above about 370 °C and especially up to about 600 °C,
can be used as a marine fuel blending component, with excellent Calculated Carbon Aromaticity Index (CCAI).
In one embodiment of the invention the marine fuel product is a blend of the obtained fraction from about 300 °C to about 370 °C, and at least part of the fraction boiling above about 370 °C, which is a fraction preferably boiling up to about 600 °C.
In one embodiment of the invention the marine fuel product comprises from 70 wt.% to 90 wt.% of a fraction boiling from about 300 °C up to about 370 °C, and from 30 wt.% to 10 wt.% of a fraction boiling above 370 °C, preferably the marine fuel product comprises from 75 wt.% to 85 wt.% of a fraction boiling from about 300 °C up to about 370 °C, and from 25 wt.% to 15 wt.% of a fraction boiling above 370 °C. The fractions are obtained by hydrotreating a feed comprising liquefied waste plastic (LWP) and a crude oil component, as herein described. In one embodiment the marine fuel product comprises or consists of 80 wt.% of a fraction boiling from about 300 °C up to about 370 °C and 20 wt.% of a fraction boiling above 370 °C, and preferably up to about 600 °C.
In one embodiment the marine fuel product, which is a blend as described above, has a cetane index of at least 57, preferably at least 59 and more preferably at least 60. The cetane index is measured (or calculated) according to 1SO4264 standard.
In addition, the marine fuel product does not only fulfil the requirements of the standard, but certain properties such as cetane index and Calculated Carbon Aromaticity Index (CCA1) are improved, when using LWP in the feed.
The cetane index especially in the fraction boiling from about 300 °C to about 370 °C increases with increased amount of LWP in feed. The cetane index increases significantly with the addition of LWP to the feed and can be at least 7 to 10 units higher even with a 20 wt.% addition of LWP compared to no LWP addition. Also, the CCA1 is improved when LWP is added to the feed. CCA1 index is an index of the ignition quality of a fuel and is significant especially for diesel engines. A lower CCA1 value means better ignition quality and CCA1 is calculated from the density and kinematic viscosity of the fuel. The CCA1 value of the marine fuel decreases with the addition of LWP to the feed. Especially the fraction boiling above about 370 °C has an improved CCA1 value.
In addition to improvements to the cetane index and CCA1, the sulfur amount is also lower when LWP is used in the feed. The yield of the fraction boiling
from about 300 °C to about 370 °C and above about 370 °C is also increased with the addition of LWP to the feed.
Especially the fraction boiling from about 300 °C to about 370 °C fulfils all requirements the ISO 8217:2017 sets on marine fuels and can therefore be used as a drop in marine fuel. Also, the fraction boiling above about 370 °C fulfils most of the requirements and is highly suitable as marine fuel or at least as a blending component for marine fuel.
In an embodiment of the current invention the marine fuel product has at least the following properties:
- a cetane index as measured according to ASTM D4737of at least 57, preferably at least 59,
- a calculated carbon aromaticity index (CCAI) according to of below 735, preferably below 730, and
- a density at 15 °C of at least 855 kg/m3.
Calculated carbon aromaticity index (CCAI) is calculated according to 1S08217:2017. Density is measured according to ISO 12185-1996.
Another object of the current invention is to provide a method for producing marine fuel. The method comprises the steps of
- obtaining a feed comprising liquefied waste plastic and a crude oil component,
- subjecting the feed to a hydrotreatment process to obtain a hydrotreated product,
- fractionating the obtained hydrotreated product to obtain at least a fraction boiling up to 370 °C and a fraction boiling above 370 °C, wherein the obtained fraction boiling up to 370 °C is collected as the marine fuel and optionally the marine fuel further comprises a part of the obtained fraction boiling above 370 °C.
In one embodiment of the method the fraction boiling up to 370 °C is a fraction boiling from 300 °C to 370 °C, and the fraction boiling above 370 °C is a fraction boiling from above 370 °C up to 600 °C.
According to the method herein described, the marine fuel is obtained by fractionating the obtained hydrotreated product to the described fractions. In one embodiment part of the fraction boiling above about 370 °C is blended to the fraction boiling from about 300 °C to about 370 °C to obtain the marine fuel. In one embodiment the method comprises blending the fractions such that the marine fuel comprises 70 wt.% to 90 wt. of the fraction boiling from about 300 °C to about
370 °C, and 30 wt.% to 10 wt.% of the fraction boiling above about 370 °C. The proportion of the fractions in the marine fuel can also be 75 wt.% to 85 wt.% and 25 wt.% to 15 wt.%, or 80 wt.% and 20 wt.% respectively.
In one embodiment of the method the hydrotreatment is a hydrodesulfurization (HDS) process. The HDS method can comprise one or more of the following:
- hydrodesulfurization is performed in the presence of a supported or unsupported catalyst, wherein the catalyst preferably comprising at least one component selected from 1UPAC group 6, 8 or 10 of the Periodic Table of Elements, more preferably the catalyst active site is Ni, Mo or Co; and preferably the support if present is alumina (AI2O3),
- a H2 to oil ratio of 150 - 400 Nm3/stdm3, preferably 180 - 250 Nm3/stdm3,
- a LHSV of 0.5 - 2.0 h 1, preferably 1.0 - 1.5 h 1,
- a temperature of 300 - 400 °C, preferably 350 - 390 °C, and
- a pressure of 4000 - 6000 kPa(a), preferably 4800-5500 kPa(a).
A further object of the invention is to provide use of liquefied waste plastic in a feed for a process producing marine fuel, wherein the process comprises hydrotreatment and fractionation to obtain at least a fraction boiling up to 370 °C and wherein the obtained fraction can be used as a whole as marine fuel or marine fuel blending component.
In one embodiment of the use the fraction boiling up to 370 °C is a fraction boiling from 300 °C to 370 °C. In one embodiment of the use a fraction boiling above 370 °C is obtained and can be used as a marine fuel blending component, preferably the fraction is boiling from above 370 °C up to 600 °C.
EXAMPLES
Example 1
A set of runs with various feeds were conducted to test the suitability of LWP as feed for producing marine fuel. The hydrodesulfurization of the various feeds was conducted in a pilot-scale reactor, which mimicked the conditions of an HDS-unit. The hydrotreatment conditions were the following: a start temperature of 350 °C, a pressure of 4500 kPa, LHSV 1.09 1/h and a H2/O11 of 280 normal L/L. A sulfidated NiMo/AhCh catalyst was used as the hydrotreating catalyst.
A set of three different feeds was used. A feed containing 100 heavy gas oil (ref) was used as a reference. One feed was prepared by adding LWP (not pretreated) to the aforementioned HGO feed in an amount of 20 wt.% (LWP1). In addition, additional feeds were prepared by adding a more pretreated LWP to the aforementioned HGO. Two feeds were prepared by either adding 10 wt.% pretreated LWP (LWP2) or 20 wt.% pretreated (LWP3) to the aforementioned HGO. Pretreatment of LWP was performed using a heat treatment in the presence of an alkaline substance.
All three feeds were hydrotreated in the same conditions using the same equipment. The hydrotreated product was fractionated and a fraction boiling from 300 °C to 370 °C and a fraction boiling above 370 °C was collected and analysed.
The results of the analyses of the two fractions are presented in tables 1 and 2 (below).
Table 1; Marine fuel properties of the hydrotreated product fraction boiling from 300 °C to 370 °C
Table 2; Marine fuel properties of the hydrotreated product fraction boiling above 370 °C
From the results presented in table 1 it can be seen that the fraction boiling from 300 °C to 370 °C fulfils all requirements for marine fuel and that the cetane index increases with addition of LWP to feed. Also, the amount of sulfur in this fraction is reduced compared to the reference when LWP is added.
The CCA1 is improved in the fraction boiling above 370 °C and the other properties of this fraction show it can be used as an marine fuel blending component.
Example 2
Blends of 300 - 370 °C and +370 °C were prepared of the fractions obtained in example 1. The blends contained 80 wt.% of the 300 - 370 °C and 20 wt.% of the +370 °C fraction. The first blend was from the 300 - 370 °C of LWP3 and +370 °C of LWP3, and the second blend was from the 300 - 370 °C of LWP3 and +370 °C of LWP1. Marine fuel properties of the two blends were analysed and is presented in Table 3 below.
The results in Table 3 show that the blends are suitable as marine fuels and have an increased cetane index compared to the reference in Tables 1 and 2.
Table 3; Marine fuel properties as well as distillation temperatures of blends of 300 - 370 °C and +370 °C fractions It will be obvious to a person skilled in the art that, as the technology advances, the inventive concept can be implemented in various ways. The invention and its embodiments are not limited to the examples described above but may vary within the scope of the claims.
Claims
1. A marine fuel product obtainable by hydrotreating a feed comprising liquefied waste plastic (LWP) and a crude oil component, wherein the hydrotreating is a hydrotreatment process followed by fractionation to obtain the marine fuel product as a fraction, and wherein the fraction obtained as marine fuel product is a fraction boiling from about 300 °C up to about 370 °C.
2. The marine fuel product according to claim 1, wherein the crude oil component is naphtha, kerosene, light gas oil (LGO), heavy gas oil (HGO), vacuum gas oil (VGO) or any mixture thereof.
3. The marine fuel product according to claim 1 or 2, wherein the feed comprises 5 wt.% to 40 wt.% liquefied waste plastic, preferably 10 wt.% to 30 wt.% liquefied waste plastic and more preferably 20 wt.% to 25 wt.% liquefied waste plastic.
4. The marine fuel product according to any one of claims 1 - 3, wherein the marine fuel product further comprises a part of a fraction boiling above about 370 °C, preferably boiling from above about 370 °C up to about 600 °C.
5. The marine fuel product according to claim 4, wherein the marine fuel product comprises from 70 wt.% to 90 wt.% of the fraction boiling from about 300 °C up to about 370 °C, and from 30 wt.% to 10 wt.% of the fraction boiling above 370 °C, preferably the marine fuel product comprises from 75 wt.% to 85 wt.% of the fraction boiling from about 300 °C up to about 370 °C, and from 25 wt.% to 15 wt.% of the fraction boiling above 370 °C.
6. The marine fuel product according to any one of claims 1 to 5, wherein the marine fuel product has a cetane index of at least 57, preferably at least 59 and more preferably at least 60.
7. The marine fuel product according to any one of the previous claims, wherein the hydrotreatment is a hydrodesulfurization (HDS) process.
8. The marine fuel product according to claim 7, wherein the hydrodesulfurization (HDS) process comprises one or more of the following:
- hydrodesulfurization is performed in the presence of a supported or unsupported catalyst, wherein the catalyst preferably comprising at least one component selected from 1UPAC group 6, 8 or 10 of the Periodic Table of Elements, more preferably the catalyst active site is Ni, Mo or Co; and preferably the support if present is alumina (AI2O3),
- a H2 to oil ratio of 150 - 400 Nm3/stdm3, preferably 180 - 250 Nm3/stdm3,
- a LHSV of 0.5 - 2.0 h 1, preferably 1.0 - 1.5 h 1,
- a temperature of 300 - 400 °C, preferably 350 - 390 °C, and
- a pressure of 4000 - 6000 kPa(a), preferably 4800-5500 kPa(a).
9. The marine fuel product according to any one of the previous claims, wherein the feed further comprises biobased material.
10. A method for producing marine fuel comprising the steps of
- obtaining a feed comprising liquefied waste plastic and a crude oil component,
- subjecting the feed to a hydrotreatment process to obtain a hydrotreated product,
- fractionating the obtained hydrotreated product to obtain at least a fraction boiling from about 300 °C up to about 370 °C and a fraction boiling above about 370 °C, wherein the obtained fraction boiling from about 300 °C up to about 370 °C is collected as the marine fuel and optionally the marine fuel comprises a part of the obtained fraction boiling above about 370 °C, preferably boiling from above about 370 °C up to about 600 °C.
11. The method of claim 10, wherein the hydrotreatment process is a hydrodesulfurization process.
12. The method according to any one of claims 10 or 11, wherein the hydrotreatment process comprises one or more of the following:
- hydrotreatment is performed in the presence of a supported or unsupported catalyst, wherein the catalyst preferably comprising at least one component selected from 1UPAC group 6, 8 or 10 of the Periodic Table of Elements, more preferably the catalyst active site is Ni, Mo or Co; and preferably the support if present is alumina (AI2O3),
- a H2 to oil ratio of 150 - 400 Nm3/stdm3, preferably 180 - 250 Nm3/stdm3,
- a LHSV of 0.5 - 2.0 h 1, preferably 1.0 - 1.5 h 1,
- a temperature of 300 - 400 °C, preferably 350 - 390 °C, and
- a pressure of 4000 - 6000 kPa(a), preferably 4800-5500 kPa(a).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20226088A FI20226088A1 (en) | 2022-12-08 | 2022-12-08 | Marine Fuel Product |
| FI20226088 | 2022-12-08 |
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| Publication Number | Publication Date |
|---|---|
| WO2024121460A1 true WO2024121460A1 (en) | 2024-06-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/FI2023/050670 WO2024121460A1 (en) | 2022-12-08 | 2023-12-08 | Marine fuel product |
Country Status (2)
| Country | Link |
|---|---|
| FI (1) | FI20226088A1 (en) |
| WO (1) | WO2024121460A1 (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20210301210A1 (en) * | 2020-03-30 | 2021-09-30 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polyethylene via refinery fcc feed pretreater and fcc units |
| WO2022144495A1 (en) * | 2020-12-30 | 2022-07-07 | Neste Oyj | Co-processing route for hydrotreating polymer waste-based material |
-
2022
- 2022-12-08 FI FI20226088A patent/FI20226088A1/en unknown
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- 2023-12-08 WO PCT/FI2023/050670 patent/WO2024121460A1/en unknown
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20210301210A1 (en) * | 2020-03-30 | 2021-09-30 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polyethylene via refinery fcc feed pretreater and fcc units |
| WO2022144495A1 (en) * | 2020-12-30 | 2022-07-07 | Neste Oyj | Co-processing route for hydrotreating polymer waste-based material |
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