[go: up one dir, main page]

WO2024155488A1 - Processus de conversion de matériau plastique en oléfines - Google Patents

Processus de conversion de matériau plastique en oléfines Download PDF

Info

Publication number
WO2024155488A1
WO2024155488A1 PCT/US2024/010992 US2024010992W WO2024155488A1 WO 2024155488 A1 WO2024155488 A1 WO 2024155488A1 US 2024010992 W US2024010992 W US 2024010992W WO 2024155488 A1 WO2024155488 A1 WO 2024155488A1
Authority
WO
WIPO (PCT)
Prior art keywords
fraction
mixture
plastic material
steam
produce
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.)
Ceased
Application number
PCT/US2024/010992
Other languages
English (en)
Inventor
Saurabh S. MADUSKAR
Bryan A. Patel
Philippe Laurent
Brenda A. Raich
James R. Lattner
Theodore W. WALKER
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.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Technology and Engineering Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ExxonMobil Technology and Engineering Co filed Critical ExxonMobil Technology and Engineering Co
Priority to EP24705851.4A priority Critical patent/EP4652238A1/fr
Priority to CN202480013699.7A priority patent/CN120731261A/zh
Publication of WO2024155488A1 publication Critical patent/WO2024155488A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/007—Visbreaking
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • This disclosure relates to processes and systems for converting one or more plastic materials to olefins. More particularly, this disclosure relates to processes and systems for processing a mixture that includes a plastic material and a carrier liquid by passing the mixture through at least one of a vis-breaker and a convection section of a stream cracking furnace to produce an effluent that includes pyrolysis oil and passing at least a portion of the effluent through a radiant section of the steam cracking furnace to produce a steam cracking effluent that includes one or more olefins.
  • plastic materials such as mechanical recycling and advanced recycling.
  • advanced recycling the plastics are broken down to smaller hydrocarbon chains and monomers that can be processed to produce various chemicals such as one or more light olefin monomers.
  • the process can include introducing a plastic material and a carrier liquid that can include a hydrocarbon into a vis-breaker. At least a portion of the plastic material can be cracked in the vis-breaker under vis-breaking conditions to produce an effluent that can include a pyrolysis oil. At least a portion of the effluent can be heated within a convection section of a steam cracking furnace and the at least a portion of the effluent can be combined with an aqueous fluid to produce a heated mixture that can include hydrocarbons and steam.
  • the heating can be carried out before, during, and/or after at least a portion of the effluent is combined with the aqueous fluid. At least a portion of the heated mixture can be steam cracked within a radiant section of the steam cracking furnace to produce a steam cracker effluent that can include one or more olefins.
  • the process for converting hydrocarbons by pyrolysis can include heating a mixture that can include a plastic material and a carrier liquid within a convection section of a steam cracking furnace and combining the mixture with an aqueous fluid to produce a heated mixture.
  • the heating can be carried out before, during, and/or after the mixture is combined with the aqueous fluid.
  • the carrier liquid can include a hydrocarbon.
  • At least a portion of the plastic material can be cracked to produce a pyrolysis oil.
  • At least a portion of the heated mixture can be steam cracked within a radiant section of the steam cracking furnace to produce a steam cracker effluent that can include one or more olefins.
  • the process for converting hydrocarbons by pyrolysis can include introducing a plastic material and a carrier liquid that can include a hydrocarbon into a vis-breaker. At least a portion of the plastic material can be cracked in the vis-breaker under vis-breaking conditions to produce an effluent that can include a pyrolysis oil.
  • a first fraction that can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof, a second fraction that can include one or more C5-C20 hydrocarbons, and, if present, a third fraction that can include one or more C21+ hydrocarbons can be separated from the effluent.
  • a hydrocarbon feed can be heated within a convection section of a steam cracking furnace and combined with an aqueous fluid to produce a heated mixture that can include hydrocarbons and steam.
  • the heating can be carried out before, during, and/or after the hydrocarbon feed is combined with the aqueous fluid.
  • At least a portion of the heated mixture and the second fraction separated from the effluent can be steam cracked within a radiant section of the steam cracking furnace to produce a steam cracker effluent that can include one or more olefins.
  • the process for converting hydrocarbons by pyrolysis can include heating a mixture that can include a plastic material and a carrier liquid within a convection section of a steam cracking furnace and combining the mixture with an aqueous fluid to produce a heated mixture.
  • the heating can be carried out before, during, and/or after the hydrocarbon feed is combined with the aqueous fluid.
  • the carrier liquid can include a hydrocarbon.
  • a portion of the plastic material can be cracked to produce a pyrolysis oil.
  • a first fraction that can include H2, one or more C1-C20 hydrocarbons, or a mixture thereof and a second fraction that can include one or more C21+ hydrocarbons can be separated from the heated mixture.
  • the second fraction can include uncracked plastic material.
  • the second fraction can be introduced into a vis-breaker. At least a portion of the uncracked plastic material can be cracked in the vis-breaker under vis-breaking conditions to produce an effluent that can include an additional quantity of pyrolysis oil.
  • a first fraction that can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof, a second fraction that can include one or more C5-C20 hydrocarbons, and, if present, a third fraction that can include one or more C21+ hydrocarbons can be separated from the effluent.
  • At least a portion of the first fraction separated from the heated mixture and the second fraction separated from the effluent can be steam cracked within a radiant section of the steam cracking furnace to produce a steam cracker effluent that can include one or more olefins.
  • FIGS. 1-6 each depict an illustrative process/system for processing a mixture that includes a plastic material and a carrier liquid in at least one of a vis-breaker and a convection section of a steam cracking furnace to produce an effluent that can include a pyrolysis oil and steam cracking at least a portion of the effluent in a radiant section of the steam cracking furnace to produce a steam cracker effluent that can include one or more olefins, according to one or more embodiments described.
  • a process is described as including at least one “step.” It should be understood that each step is an action or operation that may be carried out once or multiple times in the process, in a continuous or discontinuous fashion. Unless specified to the contrary or the context clearly indicates otherwise, multiple steps in a process may be conducted sequentially in the order as they are listed, with or without overlapping with one or more other steps, or in any other order, as the case may be. In addition, one or more or even all steps may be conducted simultaneously with regard to the same or different batch of material.
  • a second step may be carried out simultaneously with respect to an intermediate material resulting from treating the raw materials fed into the process at an earlier time in the first step.
  • the steps are conducted in the order described.
  • the indefinite article “a” or “an” shall mean “at least one” unless specified to the contrary' or the context clearly indicates otherwise.
  • embodiments using “a steam cracking furnace” include embodiments where one, two, or more steam cracking furnaces are used, unless specified to the contrary’ or the context clearly indicates that only one steam cracking furnace is used.
  • hydrocarbon as used herein means (i) any compound consisting of hydrogen and carbon atoms or (ii) any mixture of two or more such compounds in (i).
  • Cn hydrocarbon where n is a positive integer, means (i) any hydrocarbon compound comprising carbon atom(s) in its molecule at the total number of n, or (ii) any mixture of two or more such hydrocarbon compounds in (i).
  • a C2 hydrocarbon can be ethane, ethylene, acety lene, or mixtures of at least two of these compounds at any proportion.
  • a “C2 to C3 hydrocarbon” or “C2-C3 hydrocarbon” can be any of ethane, ethylene, acety lene, propane, propene, propyne, propadiene, cyclopropane, and any mixtures of two or more thereof at any proportion between and among the components.
  • a “saturated C2-C3 hydrocarbon” can be ethane, propane, cyclopropane, or any mixture thereof of two or more thereof at any proportion.
  • a “Cn+ hydrocarbon” means (i) any hydrocarbon compound comprising carbon atom(s) in its molecule at the total number of at least n, or (ii) any mixture of two or more such hydrocarbon compounds in (i).
  • a “Cn- hydrocarbon 7 ’ means (i) any hydrocarbon compound comprising carbon atoms in its molecule at the total number of at most n, or (ii) any mixture of two or more such hydrocarbon compounds in (i).
  • a “Cm hydrocarbon stream’’ means a hydrocarbon stream consisting essentially of Cm hydrocarbon(s).
  • a “Cm-Cn hydrocarbon stream” means a hydrocarbon stream consisting essentially of Cm-Cn hydrocarbon(s).
  • Crude means whole crude oil as it flows from a wellhead, a production field facility-, a transportation facility, or other initial field processing facility, optionally- including crude that has been processed by a step of desalting, treating, and/or other steps as may be necessary to render it acceptable for conventional distillation in a refinery. Crude is presumed to contain resid.
  • Crude fraction means a hydrocarbon fraction obtained via the fractionation of crude. Non-limiting examples of crudes can be or can include, but are not limited to. Tapis, Murban, Arab Light, Arab Medium, and/or Arab Heavy.
  • resid refers to a bottoms cut of a crude distillation process that contains non-volatile components. Resids are complex mixtures of heavy petroleum compounds otherwise known in the art as residuum or residual or pitch. Atmospheric resid is the bottoms product produced from atmospheric distillation of crude where a typical endpoint of the heaviest distilled product is nominally 343°C, and is referred to as 343°C resid.
  • the term “nominally”, as used herein, means that reasonable experts may disagree on the exact cut point for these terms, but by no more than +/- 55.6°C preferably no more than +/- 27.8°C.
  • Vacuum resid is the bottoms product from a distillation column operated under vacuum where the heaviest distilled product can be nominally 566°C. and is referred to as 566°C resid.
  • hydrocarbon feed refers to a composition that includes one or more hydrocarbons.
  • Illustrative hydrocarbon feeds can be or can include, but are not limited to, crude, gas oils, heating oil, jet fuel, diesel, kerosene, gasoline, coker naphtha, steam cracked naphtha, catalytically cracked naphtha, hydrocrackate, reformate, raffinate refonnate, Fischer- Tropsch liquids and/or gases, natural gasoline, distillate, virgin naphtha, atmospheric pipestill bottoms, vacuum pipestill streams such as vacuum pipestill bottoms and wide boiling range vacuum pipestill naphtha to gas oil condensates, non-virgin hydrocarbons from refineries, vacuum gas oils, heavy gas oil, naphtha contaminated with crude, atmospheric residue, heavyresidue, a CT/residue admixture, naphtha/residue admixture, hydrocarbon gases/residue admixture, hydrogen/resi
  • non-volatile components' refers to the fraction of a hydrocarbon-containing feed, e.g., a petroleum feed, having a nominal boiling point of at least 590°C, as measured by ASTM D6352-15 or D-2887-18.
  • Non-volatile components include coke precursors, which are large, condensable molecules that condense in the vapor and then form coke during steam cracking of the hydrocarbon feed.
  • coal refers to the solid or semi-solid product that can be produced during the steam cracking of hydrocarbons that includes carbon and high carbon-content organic molecules, whether produced within the convection section, radiant section, transfer lines therebetween, or within transfer lines and other equipment, e.g., a transfer line heat exchanger, dow nstream of the radiant section.
  • a "asphaltene” refers to a material obtainable from crude oil or other sources and having an initial boiling point above 650°C and which is insoluble in a paraffinic solvent.
  • a "polymer” has two or more of the same or different repeating units/mer units or simply units.
  • a "homopolymer” is a polymer having repeating units that are the same.
  • a “copolymer” is a polymer having tw o or more repeating units that are different from each other.
  • the term “copolymer” includes terpolymers (a polymer having three units that are different from each other), tetrapolymers (a polymer having four units that are different from each other), and so on.
  • the term "different” as used to refer to units indicates that the units differ from each other by at least one atom and/or are different isomerically.
  • the polymer can be or can include, but is not limited to, a nitrogen-containing polymer, a chlorine-containing polymer, a bromine-containing polymer, a fluorine-containing polymer, an oxygen-containing polymer, a polyethylene polymer, a poly propy lene polymer, a polystyrene poly mer, a butadiene polymer, an isoprene polymer, an isobutylene polymer, or any mixture thereof.
  • a nitrogen-containing polymer a chlorine-containing polymer, a bromine-containing polymer, a fluorine-containing polymer, an oxygen-containing polymer, a polyethylene polymer, a poly propy lene polymer, a polystyrene poly mer, a butadiene polymer, an isoprene polymer, an isobutylene polymer, or any mixture thereof.
  • the oxygen-containing polymer can be or can include a polyterephthalate polymer, an ethylene vinyl acetate polymer, a polycarbonate polymer, a polylactic acid polymer, an acrylate polymer, a polyoxymethylene polymer, a polyester polymer, a polyoxybenzylmethylenglycolanhydride polymer, a polyepoxide polymer, or any mixture thereof.
  • the nitrogen-containing polymer can be or can include one or more polyamide polymers, e.g., nylon; one or more polynitrile polymers, e.g., poly(acrylonitrile) and/or poly(methacrylonitrile); one or more aramids, one or more polyurethane polymers, or any mixture thereof.
  • polyamides among other mtrogen-containing polymers, also contain oxygen as part of the polymer structure.
  • a polymer that includes both oxygen and nitrogen as part of the repeat unit for forming the polymer is defined as a nitrogen-containing polymer for purposes of characterizing the plastic feedstock.
  • the chlorine- containing polymers can be or can include, but are not limited to, polyvinyl chloride (PVC) and/or polyvinylidene chloride (PVDC).
  • PVC polyvinyl chloride
  • PVDC polyvinylidene chloride
  • a polymer can be naturally occurring, modified naturally occurring, and/or synthetic.
  • plastic material refers to a composition that includes one or more polymers.
  • the plastic material comprises, consists essentially of. or consists of a synthetic polymer.
  • the plastic material comprises, consists essentially of, or consists of a used polymer.
  • the plastic material comprises, consists essentially of, or consists of one or more polymers derived from one or more olefin monomers (e.g., polyethylene, polypropylene, polyethylenepropylene, polystyrene, and the like).
  • plastic material can also include bio-derived components.
  • some types of plastic labels can include biogenic waste in the form of paper compounds.
  • 1 wt% to 25 wt% of the plastic material can correspond to bio-derived material.
  • bio-derived material can also potentially contribute to the nitrogen content of a plastic material.
  • the plastic material in addition to the one or more polymers, can also include any additives, modifiers, packaging dyes, and/or other components typically added to a polymer during and/or after formulation.
  • the plastic material can also further include any components typically found in polymer waste.
  • the plastic material alone or the plastic material mixed, blended, or otherwise combined with an optional carrier liquid is also referred to as a "heavy feed.”
  • the heavy feed may have a similar or identical composition as the hydrocarbon feed, preferably the heavy feed differs from the hydrocarbon feed.
  • the hydrocarbon feed may contain a plastic material, e.g.. the same or different plastic material contained in the heavy feed, preferably the hydrocarbon feed is substantially free, or completely free of a plastic material.
  • the hydrocarbon feed is derived from a petroleum source substantially free or completely free of a plastic material.
  • the optional “carrier liquid” disclosed herein that can be contacted with the plastic material and/or a liquid phase effluent at least partially derived from the plastic material can be or can include, but is not limited to, a wide range of petroleum or petrochemical products or streams (e.g., hydrocarbon products and/or intermediate streams produced from petroleum processing such as distillation, steam cracking, catalytic cracking, refining, and the like).
  • suitable carrier liquids can correspond to, include, comprise, consist essentially of, or consist of:
  • PAOs polyalphaolefins
  • esters such as adipate esters, phthalate esters, trimellitate esters, polyol esters (e.g., trimethylolpropane (“TMP”) esters, pentaerythritol (“PE”) esters, and blends thereof; and esters suitable for jet oils);
  • TMP trimethylolpropane
  • PE pentaerythritol
  • thermally stable liquids e.g., DOWTHERM® A available from Dow Chemical Company;
  • naphthenic and/or aromatic solvents such as toluene, benzene, methy lnaphthalene, cyclohexane, methylcy clohexane, mineral oil, or any mixture thereof;
  • the carrier liquid can be, can include, or can comprise a heat- soaked and/or hydrotreated hydrocarbon stream having an initial boiling point of at least 300°C.
  • Boiling point distributions (the distribution at atmospheric pressure) can be determined, e.g., by conventional methods such as ASTM D7500 - 15(2019) or ASTM-D86-20b.
  • a suitable heat-soaked hydrocarbon steam having an initial boiling point of at least 300°C can be produced according to the processes disclosed in WO Publication No. WO2018/111577A1.
  • a suitable hydrotreated hydrocarbon stream having an initial boiling point of at least 300°C can be produced according to the processes disclosed in WO Publication No. WO2018/111577A1.
  • a suitable heat-soaked and hydrotreated hydrocarbon stream having an initial boiling point of 300°C can be produced according to the processes disclosed in WO Publication No. WO2018/111577A1.
  • the heavy feed when the heavy feed includes the plastic material combined with the carrier liquid, the heavy feed can be in the form of a solution, slurry, suspension, dispersion, or other fluid-type phase.
  • the carrier liquid can act as a solvent.
  • aqueous fluid refers to a composition that includes water in the liquid phase, water in the vapor phase, or a mixture of water in the liquid phase and water in the vapor phase.
  • char and ash interchangeably refer to the solid or solid/liquid mixture produced during the pyrolysis of an optionally contaminated plastic material and deposited on the inner surface of a conduit or vessel, which can include organic molecules having long carbon chains and/or high boiling points such as asphaltenes, coke, organometallic compounds, inorganic materials such as metals, metallic oxides, and salts, and mixtures thereof.
  • Char and ash can be produced from the chemical reactions of the various components of a plastic material and/or introduced directly from the plastic feed material.
  • pyrolysis oil refers to a composition that includes hydrocarbons produced by at least partially cracking a plastic material.
  • ERT T exp
  • T is equal to the actual residence time in minutes
  • T is equal to the temperature in degrees Celsius
  • A is equal to 0.04745
  • B is equal to 18. 120.
  • the equivalent residence time or ERT is in seconds.
  • An "olefin” is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond.
  • olefin product’ as used herein means a product that includes an olefin, preferably a product consisting essentially of or consisting of an olefin.
  • An olefin product in the meaning of this disclosure can be, e.g., an ethylene stream, a propylene stream, a butylene stream, an ethylene/propylene mixture stream, and the like.
  • compositions, feed, effluent, product, or other stream comprises a given component at a concentration of at least 60 wt%, preferably at least 70 wt%, more preferably at least 80 wt%, more preferably at least 90 wt%, still more preferably at least 95 wt%, based on the total weight of the composition, feed, effluent, product, or other stream in question.
  • aromatic as used herein is to be understood in accordance with its art- recognized scope which includes alkyl substituted and unsubstituted mono- and poly -nuclear compounds.
  • X-rich when used in phrases such as “X-rich” or “rich in X” means, with respect to an outgoing stream obtained from a device, that the stream comprises material X at a concentration higher than in the feed material fed to the same device from which the stream is derived.
  • lean when used in phrases such as “X-lean” or “lean in X” means, with respect to an outgoing stream obtained from a device, that the stream comprises material X at a concentration lower than in the feed material fed to the same device from which the stream is derived.
  • channel and “line” are used interchangeably and mean any conduit configured or adapted for feeding, flowing, and/or discharging a vapor, a liquid, and/or a solid into the conduit, through the conduit, and/or out of the conduit, respectively.
  • a composition can be fed into the conduit, flow through the conduit, and can be discharged from the conduit to move the composition from a first location to a second location.
  • Suitable conduits can be or can include, but are not limited to, pipes, hoses, ducts, tubes, and the like.
  • wt% means percentage by weight
  • vol% means percentage by volume
  • mol% means percentage by mole
  • ppm means parts per million
  • ppm wf ’ and “wppm” are used interchangeably to mean parts per million on a weight basis. All concentrations herein are expressed on the basis of the total amount of the composition in question, unless specified otherwise. All ranges expressed herein should include both end points as two specific embodiments unless specified or indicated to the contrary.
  • a composition of a heated mixture in line 134 recovered from a convection section 132 of a steam cracking furnace 138 can be the same or different from a composition of a heated mixture in line 134 recovered from the convection section 132 of the steam cracking furnace 138 shown in any one of FIGS. 2-6.
  • FIG. 1 depicts an illustrative process/system 100 for processing a plastic material in line 102 in a vis-breaker 110 to produce an effluent in line 112 that can include a pyrolysis oil and processing at least a portion of the effluent in line 112 in a convection section 132 and a radiant section 136 of a steam cracking furnace 138 to produce a steam cracker effluent in line 140 that can include one or more olefins, according to one or more embodiments.
  • the process/system 100 can also include an optional mixing, blending, or other ‘'contact” vessel 106 and/or an optional separator 114.
  • the plastic material in line 102 can have been treated to remove at least a portion of any contaminants therefrom. In other embodiments, the plastic material in line 102 can be used as received. If the plastic material is treated to remove at least a portion of any contaminants therefrom, such treatment can include, but is not limited to, sortation, filtration, w ater washing, solvent extraction, contact with super-critical water, contact with supercritical carbon dioxide, or any combination thereof. In some embodiments, the plastic material in line 102 can have been subjected to one or more physical processes such as chopping, grinding, shredding, or other suitable process that can reduce the size of the plastic material. In some embodiments, the plastic material can have a median particle size of 10 cm or less, 3 cm or less, 2.5 cm or less, 2 cm or less, 1 cm or less, 0.1 cm or less, or 0.01 cm or less.
  • the plastic material in line 102 and a carrier liquid in line 104 can be introduced into the optional contact vessel 106 that can be configured to contact the plastic material with the earner liquid.
  • the plastic material and the carrier liquid can be actively mixed or blended via one or more agitators such as a rotating mixer inside the contact vessel 106 (not shown).
  • the contact vessel 106 can be a mixing conduit that can include one or more static mixing elements such as one or more helical fins extending from an inner surface of the conduit that can cause the plastic material to be mixed with the carrier liquid.
  • the plastic material via line 102 and the carrier liquid via line 104 can be separately introduced into the vis-breaker 110 and contacted therein.
  • the plastic material via line 102 and the carrier liquid via 104 that can be separately introduced into the vis-breaker 110 and/or a mixture of the plastic material and the carrier liquid via line 108 is introduced into the vis-breaker 110, the plastic material and the carrier liquid and/or the mixture thereof can be actively mixed or blended via one or more agitators such as a rotating mixer disposed within the vessel 106 (not shown).
  • the contact vessel 106 can be heated via one or more indirect heat exchanges that can be internal and/or external to the contact vessel 106.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can be preheated prior to introduction into the contact vessel 106.
  • the carrier liquid in line 104 can be heated to a sufficient temperature such that heat can be transferred to the plastic material.
  • the plastic material in line 102 and the carrier liquid in line 104 can be introduced into the contact vessel 106 at room temperature or a relatively low temperature, e.g., less than 50°C.
  • the contact vessel 106 can be configured to heat the plastic material and the carrier liquid to a temperature in a range from 50°C, 75°C. 100°C. or 150°C to 200°C, 275°C, or 350°C.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can be pre-heated and at a temperature in a range from 50°C, 75°C, 100°C, or 150°C to 200°C, 275°C, or 350°C when introduced into the contact vessel 106.
  • the vis-breaker 110 when the plastic material in line 102 and the carrier liquid in line 104 are introduced directly into the vis-breaker 110, the vis-breaker 110 can be heated via one or more indirect heat exchangers that can be internal and/or external to the vis-breaker 110.
  • the vis-breaker 110 can be heated by a combustion gas produced by combusting a hydrocarbon fuel that can transfer heat into the vis-breaker 110 via indirect heat transfer.
  • the carrier liquid in line 104 can be heated to a sufficient temperature such that heat can be transferred to the plastic material within the vis-breaker 110.
  • both the contact vessel 106 and the vis-breaker 110 can be configured to the heat the mixture of the plastic material and the carrier liquid therein.
  • contacting the plastic material in line 102 with the carrier liquid in line 104, whether within the contact vessel 106 and/or the vis-breaker 110 can help facilitate the flow of the plastic material by forming a mixture having a reduced viscosity or otherwise improving flow through dilution as compared to the plastic material in line 102 before combining with the carrier liquid.
  • the amount of the plastic material within the visbreaker 110 can be in a range from 0.1 wt%, 1 wt%, 3 wt%, 5, wt%, or 10 wt% to 15 wt%, 17 wt%, 20 wt%, 23 wt%, or 25 wt%. based on the combined weight of the plastic material and the carrier liquid introduced into the contact vessel 106 or the vis-breaker 110.
  • At least a portion of the plastic material can be suspended in the carrier liquid once contacted therewith such that the mixture can be in the form of a slurry.
  • at least a portion of the plastic material in the vis-breaker 110 can be at least partially melted and/or solubilized in the carrier liquid therein.
  • at least a portion of the plastic material can be subjected to vis-breaking conditions within the visbreaker 110 that can at least partially crack the plastic material such that at least a portion of the plastic material can be converted to a pyrolysis oil.
  • the pyrolysis oil in the effluent recovered via line 112 can be derived from the plastic material alone or from both the plastic material and the carrier liquid.
  • the vis-breaking conditions within the vis-breaker 110 can include heating the mixture of the plastic material and the carrier liquid at a temperature in a range from 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the vis-breaking conditions in the vis-breaker 110 can include a pressure in a range from 1,000 kPa-gauge, 1,500 kPa-gauge, 2,000 kPa-gauge, 3,000 kPa-gauge, or
  • the equivalent residence time for the plastic material in the process/system 100 can be in a range from 0.5 minutes, 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes, 60 minutes or greater.
  • the equivalent residence time can depend, at least in part, on the particular type of plastic material(s) and how fast the particular plastic material(s) can be pyrolyzed.
  • the temperature within the vis-breaker 110 and/or the amount of time required to crack a desired amount of the plastic material can widely va 7 .
  • sufficient vis-breaking of the mixture of the plastic material and possibly the carrier liquid within the vis-breaker 110 can be determined by any suitable criteria or combination of criteria such as the equivalent residence time, a viscosity' measurement of the effluent in line 112, and/or a final boiling point of the effluent in line 112.
  • suitable vis-breaking conditions and suitable vis-breakers 110 can include those described in WO Publication No. WO 1997/008266.
  • the effluent via line 112 can be introduced into the optional separator 114.
  • the separator 114 if present, can provide a first fraction via line 116, a second fraction via line 123, and, optionally, a third fraction via line 118 and/or 122.
  • the first fraction in line 116 can be or can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof.
  • the second fraction in line 123 can be or can include one or more C5-C20 hydrocarbons.
  • the third fraction in lines 118 and/or 122 can be or can include one or more C21+ hydrocarbons.
  • the separator 114 if present, can provide a vapor phase fraction via line 123, and a liquid phase fraction via line 118 and/or 122, with the first fraction in line 116 making up a portion of the vapor phase fraction in line 123.
  • the third fraction if the third fraction is recovered from the separator 114, at least a portion of the third fraction can be recycled via lines 118/120 to, if present, the contact vessel 106 and/or via lines 118/121 to the vis-breaker 110. In other embodiments, if the third fraction is recovered from the separator 114, at least a portion of the third fraction can be removed via line 122 from the process/system 100 and further processed in one or more other refinery, chemical, or other petrochemical operations and/or separated out into two or more products.
  • the third fraction if the third fraction is recovered from the separator 114, at least a portion of the third fraction can be recycled via lines 118/120 to the contact vessel 106 and/or via lines 118/121 to the vis-breaker 110 and at least a portion of the third fraction via line 122 can be removed from the process/system 100.
  • Illustrative separators 114 can include, but are not limited to, fractionation or distillation column(s), centrifuge(s), filter(s), settling drum(s), flash drum(s) ballistic separation, cyclone(s) or any combination thereof.
  • Suitable separators 114 can include those described in U.S. Patent Nos.: 6,376.732; 7,311.746; 7,427,381; 7,767,008; and 7,481,871.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can include one or more contaminants and/or include one or more compounds from which one or more contaminants can be produced or derived from when subjected to the visbreaking conditions within the vis-breaker 110.
  • an optional contaminant removal unit 124 can be used to remove at least a portion of the contaminant to produce a contaminant-lean second fraction or a contaminant-lean vapor phase that can be recovered via line 128.
  • the plastic material and/or the carrier liquid can include one or more compounds that include one or more halogen atoms, e.g., chlorine, fluorine, bromine, or a mixture thereof.
  • the plastic material can be or can include one or more halide-containing polymers and/or the plastic material can include one or more halide containing compounds disposed thereon.
  • the second fraction or the vapor phase fraction in line 123 can include one or more halide-containing compounds, e.g., HC1.
  • the second fraction or the vapor phase fraction in line 123 can be introduced into the contaminant removal unit 124 and contacted with one or more guard beds 126 disposed therein to remove at least a portion of the halide-containing compound(s) to produce a halide-lean second fraction or halide-lean vapor fraction via line 128.
  • suitable materials that can be used to make-up the guard bed 126 can be or can include, but are not limited to, alkaline or basic oxides such as calcium oxide, magnesium oxide, zinc oxide, or any mixture thereof.
  • suitable processes/systems for removing contaminants can include those disclosed in U.S. Provisional Patent Application No. 63/301,079.
  • the halide-lean second fraction or the halide-lean vapor phase fraction in line 128 can be introduced into the convection section 132 of the steam cracking furnace 134 and heated therein by flowing the second fraction through one or more conduits disposed therein.
  • the second fraction or the vapor phase fraction in line 123 can include ammonia.
  • various types of polymer additives can also include nitrogen.
  • at least a portion of the nitrogen can be converted to ammonia.
  • another type of guard bed 126 can be a guard bed configured to remove at least a portion of any ammonia that may be present in the second fraction or the vapor phase fraction in line 123.
  • adsorbents are available for the removal of ammonia, such as molecular sieve-based adsorbents.
  • the second fraction or the vapor phase fraction can include mercury.
  • the vis-breaking conditions within the vis-breaker 110 can convert at least a portion of any mercury present in the plastic material in line 102 and/or the carrier liquid in line 104 into elemental mercury.
  • another type of guard bed 126 can be a guard bed configured to remove at least a portion of any mercury' that may be present in the second fraction or the vapor phase fraction in line 123.
  • Such elemental mercury' can be removed using a mercury removal guard bed. It is noted that some guard beds suitable for mercury removal can also be suitable for silicon removal.
  • guard beds can include, but are not limited to, refractory oxides with transition metals optionally supported on the surface, such as the oxides and metals used in demetallization catalysts or a spent hydrotreating catalysts. Additionally, separate guard beds can be used for silicon and mercury removal, or separate adsorbents for silicon removal and mercury removal can be included in a single guard bed. Examples of suitable mercury adsorbents and silicon adsorbents can be or can include, but are not limited to, molecular sieves that are suitable for adsorption of mercury' and/or silicon.
  • two or more separate guard beds 126 can be used for halide, ammonia, mercury, and/or silicon removal or separate materials configured to remove one or more of a halide, ammonia, mercury, and/or silicon can be included in a single guard bed 126. While the guard bed 126 has been described with reference to solid adsorbents, it should be understood that one or more guard beds 126 can be or can include one or more non-solid guard beds such as a wash drum/vessel that can be configured for amine treating, caustic treating, and/or other treating. In some embodiments, one or more guard beds 126 can be incorporated into one or more of the processes/systems 200, 300, 400, 500, and/or 600 described below.
  • At least a portion of the second fraction or vapor phase fraction in line 123 or the contaminant-lean second fraction or contaminant-lean vapor phase fraction in line 128 can be introduced into the convection section 132 of the steam cracking furnace 138.
  • an aqueous fluid via line 130 can also be introduced into the convection section 132 and can be combined with the second fraction, the vapor phase fraction, the contaminantlean second fraction, or the contaminant-lean vapor fraction in line 123 to produce a heated mixture.
  • the aqueous fluid in line 130 can be combined with the second fraction, the vapor phase fraction, the contaminant-lean second fraction, or the contaminant-lean vapor fraction prior to introduction into the convention section 132.
  • the second fraction, the vapor phase fraction, the contaminant-lean second fraction, or the contaminant-lean vapor fraction can be partially heated within the convection section 132 by flowing through one or more conduits disposed within the convection section 132 and can then be combined with the aqueous fluid in line 130 to produce a mixture that can be further heated by flowing through one or more additional conduits disposed within the convection section 132.
  • the second fraction, the vapor phase fraction, the contaminant-lean second fraction, or the contaminantlean vapor fraction can be heated within the convection section 132 and can be combined with the aqueous fluid after exiting the convection section 132, e.g., in line 134 to produce the heated mixture.
  • heating of the second fraction, the vapor phase fraction, the contaminantlean second fraction, or the contaminant-lean vapor fraction that is introduced into the convection section 132 can be carried out before, during, and/or after the at least a portion of the second fraction, the vapor phase fraction, the contaminant-lean second fraction, or the contaminant-lean vapor fraction is combined with the aqueous fluid in line 130.
  • the heated mixture in line 134 can be at a temperature in a range 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the heated mixture in line 134 can be in the gas phase or can primarily be in the gas phase with a minor amount in the liquid phase.
  • a minor amount of the heated mixture in line 134 is in the liquid phase, such minor amount can be up to about 5 wt%, 4 wt%, 3 wt%, 2 wt%, 1 wt%, 0.5 wt%, 0. 1 wt%, or 0.01 wt%, based on the total weight of the heated mixture.
  • At least a portion of the heated mixture in line 134 can be introduced into the radiant section 136 of the steam cracking furnace 138 and steam cracked therein to produce a stream cracker effluent that can be recovered via line 140.
  • the steam cracker effluent in line 140 can include, among other products, one or more olefins, steam cracker naphtha, steam cracker gas oil, steam cracker quench oil, steam cracker tar, or any mixture thereof.
  • the steam cracking conditions within the radiant section 136 of the steam cracking furnace 138 can include, but are not limited to, one or more of: exposing the heated mixture to a temperature (as measured at a radiant outlet of the steam cracker) of > 400°C, e.g., a temperature of about 700°C, about 800°C, or about 900°C to about 950°C, about l,000°C, or about l,050°C, a pressure of about 100 kPa-absolute to about 600 kPa-absolute, and/or a steam cracking residence time of about 0.01 seconds to about 5 seconds.
  • the heated mixture can be steam cracked according to the processes and systems disclosed in U.S. Patent Nos.
  • the steam cracker effluent in line 140, at an outlet of the radiant section 136, can be at a temperature of > 400°C, e.g., a temperature of 700°C, 800°C, or 900°C to 950°C, l,000°C, or l,050°C.
  • the vis-breaker 110 is shown to be connected with a single steam cracking furnace 138. It is further contemplated that, in certain preferred embodiments, the vis-breaker 110 may be connected with multiple steam cracking furnaces. For example, in one embodiment (not shown), a split stream of the effluent in line 112, the second fraction or vapor phase fraction in line 123. or the contaminant-lean second fraction or the contaminant-lean vapor phase fraction in line 128 may be sent to a heat exchanger located in the convection section of a second steam cracking furnace (not shown), where it is combined with another aqueous fluid and heated and sent to a radiant section of the second steam cracking furnace.
  • Such multiple steam cracking furnace arrangement can ensure continued plastic pyrolysis and steam cracking operation even if one steam cracking furnace stopped operation due to, e.g.. decoking or other needs.
  • a single vis-breaker 110 is shown to be connected with a single steam cracking furnace 138. It is further contemplated that, in certain preferred embodiments, multiple visbreakers 110, of the same, similar, or differing sizes and/or designs, may be connected with one or multiple steam cracking furnaces.
  • one vis-breaker can be designed and configured to accept a first type of plastic material
  • a second vis-breaker can be designed to accept a second t pe of plastic material, which may be the same or different from the first plastic material.
  • the two vis-breakers can be operated under differing vis-breaking conditions to suit the needs of the differing plastic materials.
  • the second fraction exiting the two vis-breakers can be combined and then fed into the convection section(s) of one or more steam cracking furnaces optionally together with an additional hydrocarbon stream.
  • the second fraction exiting the two vis-breakers if differing substantially in terms of temperature and/or composition, may be separately introduced into separate heat exchangers disposed within the convection section(s) of one or more steam cracking furnaces, and then introduced to the same or different radiant section of one or more steam cracking furnaces.
  • Such embodiments including multiple visbreakers can have the advantage of being capable of handling multiple differing plastic materials requiring differing pyrolysis conditions.
  • the steam cracking furnace 138 can be operated on all hydrocarbon feeds that can be processed in a steam cracking furnace.
  • the steam cracking furnace 138 can be operated exclusively on one or more feeds thereto that are gaseous at room temperature, e.g., ethane, propane, and/or butane, one or more feeds that are liquid at room temperature, e.g.. naphtha, one or more feeds that are solid at room temperature, e.g., heavy fractions obtained from a crude oil, or any combination or mixture thereof.
  • the steam cracking furnace may be operated to combust any fuel suitable for a steam cracking furnace to generate the thermal energy required for the pyrolysis of hydrocarbon molecules in the radiant section of the furnace.
  • fuel can include, e.g., methane, natural gas, hydrogen, and mixtures thereof at any proportion.
  • FIG. 2 depict an illustrative process/system 200 for processing a plastic material in line 102 in a vis-breaker 110 to produce an effluent in line 112 that can include a pyrolysis oil and processing at least a portion of the effluent in line 112 in a convection section 132 and a radiant section 136 of a steam cracking furnace 138 to produce a steam cracker effluent in line 140 that can include one or more olefins, according to one or more embodiments.
  • the process/system 200 can also include an optional contact vessel 106 and/or an optional separator 114.
  • the process/system 200 is similar to the process/system 100, with the main difference being that the process/system 200 further includes a separation drum 202 configured to separate a vapor phase fraction and a liquid phase fraction from the heated mixture in line 134.
  • the vapor phase fraction can be recovered via line 204 from the separation drum 202.
  • At least a portion of the vapor phase fraction via line 204 can be introduced into the radiant section 136 of the steam cracking furnace 138 to produce a steam cracker effluent via line 140 that can include one or more olefins, as described above with reference to FIG. 1.
  • the liquid phase fraction can be recovered via line 206 and/or line 208. In some embodiments, at least a portion of the liquid phase fraction can be recycled to the optional contact vessel 106 and/or to the vis-breaker 110 (not shown). In some embodiments, at least a portion of the liquid phase fraction can be removed via line 208 from the process/system 200 and further processed in one or more other refinery, chemical, or other petrochemical operations and/or separated out into two or more products. In still other embodiments, a first portion of the liquid phase fraction can be recycled via line 206 to the optional contact vessel 106 and/or the vis-breaker 110 and a second portion can be removed via line 208 from the process 200.
  • the separation drum 202 can also be referred to as a vapor-liquid separator, vaporization drum, or flash drum.
  • the liquid phase fraction in line 206 and/or 208 can have a cutoff point of from 300°C to 700°C, e.g., 310°C to 550°C, as measured according to ASTM DI 160-18, ASTM D-86-20b, or ASTM D2887-19ae2.
  • Conventional separation drums can be utilized to do this, though the invention is not limited thereto. Examples of such conventional separation drums can include those disclosed in U.S. Patent Nos.
  • the equivalent residence time for the plastic material in the process/system 200 can be in a range from 0.5 minutes. 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes, 60 minutes or greater.
  • the system 200 can also include one or more contaminant removal units 124 as described above with reference to FIG. 1.
  • the second fraction or the vapor phase fraction via line 123 can be processed within one or more contaminant removal units to produce a contaminant-lean second fraction or a contaminantlean vapor phase fraction that can be introduced into the convection section 132 of the steam cracking furnace 138.
  • FIG. 3 depicts an illustrative process/system 300 for processing a plastic material in line 102 and a carrier liquid in line 104 in a convection section 132 of a steam cracking furnace 138 to produce a heated mixture in line 134 that can include a pyrolysis oil and processing at least a portion of the heated mixture in line 134 in a radiant section 136 of the steam cracking furnace 138 to produce a steam cracker effluent in line 140 that can include one or more olefins, according to one or more embodiments.
  • the process/system 300 can also include an optional mixing, blending, or other contact vessel 106 and/or an optional a separation drum 202.
  • the plastic material in line 102 and a carrier liquid in line 104 can be directly introduced into the convection section 132 of the steam cracking furnace 138 and contacted therein to produce a mixture or can be combined within the optional contact vessel 106 and a mixture that includes the plastic material and the carrier liquid via line 108 can be introduced into the convection section 132 of the steam cracking furnace 138.
  • the amount of the plastic material in the mixture can be in a range from 0.
  • an aqueous fluid via line 130 can also be introduced into the convection section 132 and can be combined with the mixture that includes the plastic material and the carrier liquid before, during, or after the mixture is heated within the convection section 132 to produce a heated mixture via line 134.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can include a sufficient amount of aqueous fluid that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • an aqueous fluid can be introduced into the contact vessel 106 such that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • At least a portion of the plastic material can be cracked within the convection section 132 of the steam cracking furnace 138 to produce the pyrolysis oil.
  • the heated mixture in line 134 can be at a temperature in a range 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the heated mixture in line 134 can be a vapor/liquid mixture.
  • the heated mixture in line 134 can be introduced into the separation drum 202 to produce a vapor phase fraction via line 204 and a liquid phase fraction via line 206 and/or 208.
  • at least a portion of the liquid phase fraction can be recycled to the contact vessel 106 (if present) and/or to the convection section 132 of the steam cracking furnace.
  • At least a portion of the vapor phase fraction via line 204 can be introduced into and steam cracked within the radiant section 136 of the steam cracking furnace 138 to produce the steam cracker effluent via line 140 that can include one or more olefins.
  • the heated mixture in line 134 can be in the gas phase or can primarily be in the gas phase with a minor amount in the liquid phase.
  • a minor amount of the heated mixture in line 134 can be up to about 5 wt%, 4 wt%, 3 wt%, 2 wt%, 1 wt%, 0.5 wt%, 0. 1 wt%, or 0.01 wt%, based on the total weight of the heated mixture.
  • the heated mixture via line 134 can be introduced directly into the radiant section 136 of the steam cracking furnace 138 to produce the steam cracker effluent via line 140 that can include one or more olefins.
  • a vis-breaker is not needed to crack the plastic material. Rather heat from the convection section 132 of the steam cracking furnace 138 can be sufficient to convert a desired amount of the plastic material in line 102 into pyrolysis oil that can be steam cracked within the radiant section 136 of the steam cracking furnace 138.
  • the plastic material in line 102 can include primarily light polymers that can more readily be cracked under the conditions present within the convection section 132 and/or the amount of plastic material combined with the carrier liquid in line 104 can be relatively low such that essentially all the plastic material can be cracked within the convection section 132 of the steam cracking furnace 138.
  • the heated mixture in line 134 includes the liquid phase fraction
  • recycling at least a portion of the liquid phase fraction can increase the equivalent residence time of the plastic material subjected to the heat within the convection section 132 to crack a sufficient amount of the plastic material.
  • the convection section process conditions in the convection section 132 can include an equivalent residence time in the convection section 132 sufficient to crack at least a portion of the plastic material to produce the pyrolysis oil.
  • the equivalent residence time for the plastic material in the process/system 300 can be in a range from 0.5 minutes, 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes, 60 minutes or greater.
  • the system 300 can also include one or more contaminant removal units 124 as described above with reference to FIG. 1.
  • the heated mixture (when in the gas phase or primarily in the gas phase) via line 134 or the vapor phase fraction via line 204 can be processed within the one or more contaminant removal units to produce a contaminant-lean heated mixture or a contaminant-lean vapor phase fraction that can be introduced into the radiant section 136 of the steam cracking furnace 138 and steam cracked therein to produce the steam cracker effluent via line 140.
  • FIG. 4 depicts an illustrative process/system 400 for processing a plastic material in line 102 and a carrier liquid in line 104 in a convection section 132 of a steam cracking furnace 138, a vis-breaker 110, and a radiant section 136 of the steam cracking furnace 138 to produce a steam cracker effluent via line 140 that can include one or more olefins, according to one or more embodiments.
  • the process/system 400 can also include an optional contact vessel 106 and/or an optional separator 114.
  • the plastic material in line 102 and a carrier liquid in line 104 can be directly introduced into the convection section 132 of the steam cracking furnace 138 and contacted therein to produce a mixture or can be combined within the optional contact vessel 106 and a mixture that includes the plastic material and the carrier liquid via line 108 can be introduced into the convection section 132 of the steam cracking furnace 138.
  • the amount of the plastic material in the mixture can be in a range from 0.
  • an aqueous fluid via line 130 can also be introduced into the convection section 132 and can be combined with the mixture that includes the plastic material and the carrier liquid before, during, or after the mixture is heated within the convection section 132 to produce a heated mixture via line 134.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can include a sufficient amount of aqueous fluid that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • an aqueous fluid can be introduced into the contact vessel 106 such that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • the mixture of the plastic material, carrier liquid, and aqueous fluid can be heated within the convection section 132 of the steam cracking furnace 138 to produce a heated mixture via line 134. At least a portion of the plastic material can be cracked within the convection section 132 to produce a pyrolysis oil.
  • the heated mixture in line 134 can include pyrolysis oil.
  • the heated mixture in line 134 can be at a temperature in a range 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the heated mixture via line 134 can be introduced into the vis-breaker 110. At least a portion of any remaining plastic material present in the heated mixture in line 134 can be cracked under vis-breaking conditions within the vis-breaker 110 to produce an effluent in line 112 that can include additional pyrolysis oil.
  • an additional carrier liquid via line 404 can be introduced into the vis-breaker 110. If the additional carrier liquid via line 404 is introduced into the vis-breaker 110, the additional carrier liquid can be the same or different from the carrier liquid introduced via line 104 into the convection section 132 of the steam cracking furnace 138.
  • the effluent via line 112 can be introduced into the optional separator 114.
  • the separator 114 can separate a first fraction that can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof, a second fraction that can include one or more C5-C20 hydrocarbons, and. if present, a third fraction that can include one or more C21+ hydrocarbons from the effluent.
  • the first fraction can be recovered via line 116
  • the second fraction can be recovered via line 123
  • the third fraction via line 118 and/or 122 can be recovered from the separator 114.
  • the third fraction if the third fraction is separated from the effluent, at least a portion of the third fraction can be recycled to the contact vessel 106 via lines 118/120, at least a portion of the third fraction can be recycled to the vis-breaker via lines 118/121, and/or at least a portion of the third fraction can be removed via line 122 from the process/system 400 and further processed in one or more other refinery, chemical, or other petrochemical operations and/or separated out into two or more products.
  • the separator 114 if present, can provide a vapor phase fraction via line 123, and a liquid phase fraction via line 118 and/or 122, with the first fraction in line 116 making up a portion of the vapor phase fraction in line 123.
  • At least a portion of the second fraction or the vapor phase fraction via line 123 can be introduced into the radiant section 136 of the steam cracker furnace 138 and can be steam cracked therein to produce the steam cracker effluent via line 140 that can include one or more olefins.
  • the equivalent residence time for the plastic material in the process/system 400 can be in a range from 0.5 minutes, 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes. 60 minutes or greater.
  • the system 400 can also include one or more contaminant removal units 124 as described above with reference to FIG. 1.
  • the second fraction or the vapor phase fraction via line 123 can be processed within one or more contaminant removal units to produce a contaminant-lean second fraction or a contaminantlean vapor phase fraction that can be introduced into the radiant section 136 of the steam cracking furnace 138 and steam cracked therein to produce the steam cracker effluent via line 140.
  • FIG. 5 depicts an illustrative process/system 500 for processing a plastic material in line 102 in a vis-breaker 110 to produce an effluent via line 112, processing a hydrocarbon feed in line 502 and an aqueous fluid in line 130 within a convection section 132 of a steam cracking furnace 138 to produce a heated mixture via line 134, and processing at least a portion of the effluent in line 112 and at least a portion of the heated mixture in line 134 within a radiant section 136 of the steam cracking furnace 138 to produce a steam cracker effluent via line 140 that can include one or more olefins, according to one or more embodiments.
  • the process/system 500 can also include an optional contact vessel 106, an optional separator 114, and/or an optional separation drum 202.
  • the plastic material via line 102 and a carrier liquid via line 104 can be introduced into the vis-breaker 110 or can be combined within the optional contact vessel 106 and a mixture that includes the plastic material and the carrier liquid via line 108 can be introduced into the vis-breaker 110.
  • the amount of the plastic material in the mixture can be in a range from 0. 1 wt%, 1 wt%, 3 wt%, 5, wt%, or 10 wt% to 15 wt%, 17 wt%, 20 wt%, 23 wt%, or 25 wt%, based on the combined weight of the plastic material and the carrier liquid introduced into the contact vessel 106 or the vis-breaker 110.
  • the mixture of the plastic material and the carrier liquid can be subjected to vis-breaking conditions within the visbreaker 110 sufficient to crack at least a portion of the plastic material to produce an effluent via line 112 that can include pyrolysis oil.
  • the effluent via line 112 can be introduced into the optional separator 114.
  • the separator 114 can separate a first fraction that can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof, a second fraction that can include one or more C5-C20 hydrocarbons, and, if present, a third fraction that can include one or more C21+ hydrocarbons from the effluent.
  • the first fraction can be recovered via line 116
  • the second fraction can be recovered via line 123
  • the third fraction via line 118 and/or 122 can be recovered from the separator 114.
  • the third fraction if the third fraction is separated from the effluent, at least a portion of the third fraction can be recycled to the contact vessel 106 via lines 118/120, at least a portion of the third fraction can be recycled to the vis-breaker via lines 118/121, and/or at least a portion of the third fraction can be removed via line 122 from the process/system 500 and further processed in one or more other refiner ⁇ ’, chemical, or other petrochemical operations and/or separated out into two or more products.
  • the separator 114 if present, can provide a vapor phase fraction via line 123, and a liquid phase fraction via line 118 and/or 122, with the first fraction in line 116 making up a portion of the vapor phase fraction in line 123.
  • At least a portion of the second fraction or the vapor phase fraction via line 123 can be introduced into the radiant section 136 of the steam cracking furnace 138 and can be steam cracked therein to produce a first portion of the steam cracker effluent via line 140 that can include one or more olefins.
  • the hydrocarbon feed via line 502 and the aqueous fluid via line 130 can be introduced into the convection section 132 of the steam cracking furnace 138 and heated therein to produce the heated mixture in line 134 that can include hydrocarbons and steam.
  • the aqueous fluid in line 130 can be combined with the hydrocarbon feed before, during, or after the hydrocarbon feed is heated within the convection section 132 to produce the heated mixture via line 134.
  • the heated mixture in line 134 can be at a temperature in a range 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the heated mixture in line 134 can be in the gas phase or can primarily be in the gas phase with a minor amount in the liquid phase.
  • a minor amount of the heated mixture in line 134 when a minor amount of the heated mixture in line 134 is in the liquid phase, such minor amount can be up to about 5 wt%, 4 wt%, 3 wt%, 2 wt%, 1 wt%, 0.5 wt%, 0.1 wt%, or 0.01 wt%, based on the total weight of the heated mixture.
  • at least a portion of the heated mixture in line 134 can be introduced into the radiant section 136 of the steam cracking furnace 138 and cracked therein to produce a second portion of the steam cracker effluent via line 140 that includes one or more olefins.
  • the heated mixture in line 134 can be a vapor/liquid mixture.
  • the heated mixture in line 134 can be introduced into the separation drum 202 to produce a vapor phase fraction via line 204 and a liquid phase fraction via line 206 and/or line 208.
  • At least a portion of the vapor phase fraction via line 204 can be introduced into and steam cracked within the radiant section 136 of the steam cracking furnace to produce the second portion of the steam cracker effluent via line 140 that can include one or more olefins.
  • At least a portion of the liquid phase fraction via line 206 can be introduced to the contact vessel (when present) 106, as shown, and/or the vis-breaker 110 (not shown), and/or recycled to the convection section 132 of the steam cracking furnace 138 (not show n).
  • at least a portion of the liquid phase fraction can be removed via line 208 from the process/system 500 and further processed in one or more other refinery, chemical, or other petrochemical operations and/or separated out into two or more products.
  • a first portion of the liquid phase fraction can be introduced via line 206 to the optional contact vessel 106 and/or the vis-breaker 110 and/or recycled to the convection section 132 and a second portion can be removed via line 208 from the process/system 500.
  • the equivalent residence time for the plastic material in the process/system 500 can be in a range from 0.5 minutes. 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes, 60 minutes or greater.
  • the second fraction or the vapor phase fraction in line 123 and the heated mixture in line 134 or the vapor phase fraction in line 204 steam cracked within the radiant section 136 to produce the first portion and the second portion of the steam cracker effluent can be recovered as a mixture via line 140.
  • the second fraction or the vapor phase fraction in line 123 and the heated mixture in line 134 or the vapor phase fraction in line 204 can be combined with one another to produce a mixture that can be steam cracked within the radiant section 136 of the steam cracking furnace to produce the steam cracker effluent in line 140.
  • the second fraction or the vapor phase fraction in line 123 and the heated mixture in line 134 or the vapor phase fraction in line 204 can be steam cracked within separate tubes disposed within the radiant section 136 of the steam cracking furnace 138.
  • the steam cracker effluents recovered from the separate tubes can be combined with one another to produce the steam cracker effluent in line 140.
  • the steam cracker effluents recovered from the separate tubes can be maintained as separate steam cracker effluents rather than combining the two.
  • the system 500 can also include one or more contaminant removal units 124 as described above with reference to FIG. 1.
  • the second fraction or the vapor phase fraction via line 123 can be processed within one or more contaminant removal units to produce a contaminant-lean second fraction or a contaminantlean vapor phase fraction that can be introduced into the radiant section 136 of the steam cracking furnace 138 and steam cracked therein to produce the steam cracker effluent via line 140.
  • FIG. 6 depicts an illustrative process/system 600 for processing a plastic material in line 102 and a carrier liquid in line 104 in a convection section 132 of a steam cracking furnace 138 to produce a heated mixture in line 134, introducing a first portion of the heated mixture via line 204 into a radiant section 136 of the steam cracking furnace 138 to produce a first portion of a steam cracker effluent in line 140, introducing a second portion of the heated mixture via line 206 into a vis-breaker 110 to produce an effluent in line 112, and introducing at least a portion of the effluent via line 123 into the radiant section 136 of the steam cracking furnace 138 to produce a second portion of the steam cracker effluent in line 140.
  • the process/system 300 can also include an optional contact vessel 106 and/or an optional separation drum 202.
  • the plastic material in line 102 and a carrier liquid in line 104 can be directly introduced into the convection section 132 of the steam cracking furnace 138 and contacted therein to produce a mixture or can be combined within the optional contact vessel 106 and a mixture that includes the plastic material and the carrier liquid via line 108 can be introduced into the convection section 132 of the steam cracking furnace 138.
  • the amount of the plastic material in the mixture can be in a range from 0.
  • an aqueous fluid via line 130 can also be introduced into the convection section 132 and can be combined with the mixture that includes the plastic material and the carrier liquid before, during, or after the mixture is heated within the convection section 132 to produce the heated mixture via line 134.
  • the plastic material in line 102 and/or the carrier liquid in line 104 can include a sufficient amount of aqueous fluid that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • an aqueous fluid can be introduced into the contact vessel 106 such that the addition of the aqueous fluid via line 130 can be reduced or avoided.
  • At least a portion of the plastic material can be cracked within the convection section 132 of the steam cracking furnace 138 to produce a pyrolysis oil.
  • the heated mixture in line 134 can include pyrolysis oil.
  • the heated mixture in line 134 can be at a temperature in a range 300°C, 350°C, 375°C, or 400°C to 425°C, 450°C, 475°C, 525°C, 550°C, or 600°C.
  • the heated mixture in line 134 can be a vapor/liquid mixture.
  • the heated mixture in line 134 can be introduced into the separation drum 202 to produce a vapor phase fraction or first fraction via line 204 and a liquid phase fraction or second fraction via line 206 and/or 208.
  • the vapor phase or first fraction in line 204 can include H2, one or more C1-C20 hydrocarbons, or a mixture thereof.
  • the liquid phase or second fraction in line 206 and/or 208 can include one or more C21+ hydrocarbons, where the second fraction includes uncracked plastic material.
  • At least a portion of the vapor phase or first fraction via line 204 can be introduced into the radiant section 136 of the steam cracking furnace 138 to produce a first portion of the steam cracker effluent in line 140 that can include one or more olefins.
  • at least a portion of the liquid phase or second fraction via line 206 can be introduced into the vis-breaker 110.
  • At least a portion of the uncracked plastic material can be cracked in the vis- breaker under vis-breaking conditions to produce an effluent via line 112 that can include an additional quantity of pyrolysis oil.
  • an additional carrier liquid via line 404 can be introduced into the vis-breaker 110.
  • the additional carrier liquid via line 404 can be the same or different from the carrier liquid introduced via line 104 into the convection section 132 of the steam cracking furnace 138.
  • at least a portion of the liquid phase or second fraction via line 206 can be recycled to the contact vessel 106 and/or the convection section 132. If at least a portion of the liquid phase or second fraction via line 206 is recycled to the contact vessel and/or the convection section 132, at least a portion of the uncracked plastic material can be cracked within the convection section 132 to produce another additional quantity of pyrolysis oil.
  • the effluent via line 112 can be introduced into the optional separator 114.
  • the separator 114 can separate a first fraction that can include H2, one or more C1-C4 hydrocarbons, or a mixture thereof, a second fraction that can include one or more C5-C20 hydrocarbons, and. if present, a third fraction that can include one or more C21+ hydrocarbons from the effluent.
  • the first fraction can be recovered via line 116
  • the second fraction can be recovered via line 123
  • the third fraction via line 118 and/or 122 can be recovered from the separator 114.
  • the third fraction if the third fraction is separated from the effluent, at least a portion of the third fraction can be recycled to the contact vessel 106 via lines 118/120, the convection section 132 (not shown), at least a portion of the third fraction can be recycled to the vis-breaker via lines 118/121, and/or at least a portion of the third fraction can be removed via line 122 from the process/system 500 and further processed in one or more other refinery, chemical, or other petrochemical operations and/or separated out into two or more products.
  • the separator 114 if present, can provide a vapor phase fraction via line 123, and a liquid phase fraction via line 118 and/or 122, with the first fraction in line 116 making up a portion of the vapor phase fraction in line 123.
  • the equivalent residence time for the plastic material in the process/system 600 can be in a range from 0.5 minutes, 1 minute, 2 minutes, or 3 minutes to 5 minutes, 10 minutes, 30 minutes, 60 minutes or greater.
  • At least a portion of the second fraction or the vapor phase fraction via line 123 can be introduced into the radiant section 136 of the steam cracking furnace 138 and can be steam cracked therein to produce a second portion of the steam cracker effluent via line 140 that can include one or more olefins.
  • the second fraction or the vapor phase fraction in line 123 and the vapor phase fraction in line 204 can be combined with one another to produce a mixture that can be steam cracked within the radiant section 136 of the steam cracking furnace 138 to produce the steam cracker effluent in line 140.
  • the second fraction or the vapor phase fraction in line 123 and the vapor phase fraction in line 204 can be steam cracked within separate tubes disposed within the radiant section 136 of the steam cracking furnace 138.
  • the steam cracker effluents recovered from the separate tubes can be combined with one another to produce the steam cracker effluent in line 140.
  • the steam cracker effluents recovered from the separate tubes can be maintained as separate steam cracker effluents rather than combining the two.
  • the system 600 can also include one or more contaminant removal units 124 as described above with reference to FIG. 1.
  • the second fraction or the vapor phase fraction via line 123 can be processed within one or more contaminant removal units to produce a contaminant-lean second fraction or a contaminantlean vapor phase fraction that can be introduced into the radiant section 136 of the steam cracking furnace 138 and steam cracked therein to produce the steam cracker effluent via line.
  • This guideline can be used to identify the equivalent seventy preferred for any combination of visbreaker and convection sections as pre-processors to convert waste plastic into pyrolysis products and then ultimately produce olefins by feeding those products to the radiant section of the steam cracking furnace.
  • an equivalent residence time of about 600 seconds at a temperature of about 427°C (about 800°F) is sufficient to convert about 90% of the high- density polyethylene to a feed suitable for introducing into the radiant section of the steam cracking furnace.

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)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne des processus et des systèmes de conversion d'hydrocarbures par pyrolyse. Dans certains modes de réalisation, un matériau plastique et un liquide porteur qui peuvent comprendre un hydrocarbure peuvent être introduits dans un brise-vis. Au moins une partie du matériau plastique peut être craquée dans le brise-vis dans des conditions de rupture de vis pour produire un effluent qui peut comprendre une huile de pyrolyse. Au moins une partie de l'effluent peut être chauffée à l'intérieur d'une section de convection d'un four de vapocraquage et combinée à un fluide aqueux pour produire un mélange chauffé qui peut comprendre des hydrocarbures et de la vapeur. Le chauffage peut être effectué avant, pendant et/ou après que la ou les parties de l'effluent sont combinées avec le fluide aqueux. Au moins une partie du mélange chauffé peut être craquée à la vapeur à l'intérieur d'une section rayonnante du four de vapocraquage pour produire un effluent de vapocraqueur comprenant une ou plusieurs oléfines.
PCT/US2024/010992 2023-01-19 2024-01-10 Processus de conversion de matériau plastique en oléfines Ceased WO2024155488A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP24705851.4A EP4652238A1 (fr) 2023-01-19 2024-01-10 Processus de conversion de matériau plastique en oléfines
CN202480013699.7A CN120731261A (zh) 2023-01-19 2024-01-10 将塑料材料转化成烯烃的方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202363480646P 2023-01-19 2023-01-19
US63/480,646 2023-01-19

Publications (1)

Publication Number Publication Date
WO2024155488A1 true WO2024155488A1 (fr) 2024-07-25

Family

ID=89977695

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2024/010992 Ceased WO2024155488A1 (fr) 2023-01-19 2024-01-10 Processus de conversion de matériau plastique en oléfines

Country Status (3)

Country Link
EP (1) EP4652238A1 (fr)
CN (1) CN120731261A (fr)
WO (1) WO2024155488A1 (fr)

Citations (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4827064A (en) 1986-12-24 1989-05-02 Mobil Oil Corporation High viscosity index synthetic lubricant compositions
US5264642A (en) 1992-06-19 1993-11-23 Mobil Oil Corp. Molecular weight control of olefin oligomers
DE4329435C1 (de) * 1993-09-01 1994-12-22 Leuna Werke Gmbh Verfahren zur rohstofflichen Verwertung von Altkunststoffen oder Altkunststoffgemischen
WO1997008266A1 (fr) 1995-08-22 1997-03-06 Mobil Oil Corporation Procede de viscoreduction utilisant des plastiques en tant que matiere de depart associee
US6376732B1 (en) 2000-03-08 2002-04-23 Shell Oil Company Wetted wall vapor/liquid separator
US6419885B1 (en) 1997-06-10 2002-07-16 Exxonmobil Chemical Patents, Inc. Pyrolysis furnace with an internally finned U shaped radiant coil
US7097758B2 (en) 2002-07-03 2006-08-29 Exxonmobil Chemical Patents Inc. Converting mist flow to annular flow in thermal cracking application
US7138047B2 (en) 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US7220887B2 (en) 2004-05-21 2007-05-22 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking hydrocarbon feedstock containing resid
US7235705B2 (en) 2004-05-21 2007-06-26 Exxonmobil Chemical Patents Inc. Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks
US7244871B2 (en) 2004-05-21 2007-07-17 Exxonmobil Chemical Patents, Inc. Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids
US7247765B2 (en) 2004-05-21 2007-07-24 Exxonmobil Chemical Patents Inc. Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel
US7297833B2 (en) 2004-05-21 2007-11-20 Exxonmobil Chemical Patents Inc. Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7312371B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7311746B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid
US7351872B2 (en) 2004-05-21 2008-04-01 Exxonmobil Chemical Patents Inc. Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace
US7481871B2 (en) 2004-12-10 2009-01-27 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus
US7488459B2 (en) 2004-05-21 2009-02-10 Exxonmobil Chemical Patents Inc. Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking
US7674366B2 (en) 2005-07-08 2010-03-09 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7820035B2 (en) 2004-03-22 2010-10-26 Exxonmobilchemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US8105479B2 (en) 2009-06-18 2012-01-31 Exxonmobil Chemical Patents Inc. Process and apparatus for upgrading steam cracker tar-containing effluent using steam
EP2828367A1 (fr) 2012-03-22 2015-01-28 ExxonMobil Research and Engineering Company Nouvelle combinaison antioxydante et huiles de base synthétiques la contenant
US9365788B2 (en) 2011-10-10 2016-06-14 Exxonmobil Chemical Patents Inc. Process to produce improved poly alpha olefin compositions
US9409834B2 (en) 2005-07-19 2016-08-09 Exxonmobil Chemical Patents Inc. Low viscosity poly-alpha-olefins
US9637694B2 (en) 2014-10-29 2017-05-02 Exxonmobil Chemical Patents Inc. Upgrading hydrocarbon pyrolysis products
US9777227B2 (en) 2014-04-30 2017-10-03 Exxonmobil Chemical Patents Inc. Upgrading hydrocarbon pyrolysis products
WO2018111577A1 (fr) 2016-12-16 2018-06-21 Exxonmobil Chemical Patents Inc. Valorisation de goudron de pyrolyse
WO2018111574A1 (fr) 2016-12-16 2018-06-21 Exxonmobil Chemical Patents Inc. Prétraitement de goudron de pyrolyse
US20180170832A1 (en) 2016-12-20 2018-06-21 Exxonmobil Chemical Patents Inc. Process for Steam Cracking Hydrocarbons
WO2021204818A1 (fr) * 2020-04-07 2021-10-14 Total Research & Technology Feluy Valorisation d'huile à base de déchets plastiques en produits chimiques à valeur élevée par craquage catalytique direct

Patent Citations (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4827064A (en) 1986-12-24 1989-05-02 Mobil Oil Corporation High viscosity index synthetic lubricant compositions
US5264642A (en) 1992-06-19 1993-11-23 Mobil Oil Corp. Molecular weight control of olefin oligomers
DE4329435C1 (de) * 1993-09-01 1994-12-22 Leuna Werke Gmbh Verfahren zur rohstofflichen Verwertung von Altkunststoffen oder Altkunststoffgemischen
WO1997008266A1 (fr) 1995-08-22 1997-03-06 Mobil Oil Corporation Procede de viscoreduction utilisant des plastiques en tant que matiere de depart associee
US6419885B1 (en) 1997-06-10 2002-07-16 Exxonmobil Chemical Patents, Inc. Pyrolysis furnace with an internally finned U shaped radiant coil
US6376732B1 (en) 2000-03-08 2002-04-23 Shell Oil Company Wetted wall vapor/liquid separator
US7097758B2 (en) 2002-07-03 2006-08-29 Exxonmobil Chemical Patents Inc. Converting mist flow to annular flow in thermal cracking application
US7138047B2 (en) 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US7578929B2 (en) 2002-07-03 2009-08-25 Exxonmoil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US7820035B2 (en) 2004-03-22 2010-10-26 Exxonmobilchemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
US7427381B2 (en) 2004-05-21 2008-09-23 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid
US7247765B2 (en) 2004-05-21 2007-07-24 Exxonmobil Chemical Patents Inc. Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel
US7297833B2 (en) 2004-05-21 2007-11-20 Exxonmobil Chemical Patents Inc. Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7312371B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7311746B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid
US7351872B2 (en) 2004-05-21 2008-04-01 Exxonmobil Chemical Patents Inc. Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace
US7244871B2 (en) 2004-05-21 2007-07-17 Exxonmobil Chemical Patents, Inc. Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids
US7993435B2 (en) 2004-05-21 2011-08-09 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking hydrocarbon feedstock containing resid
US7488459B2 (en) 2004-05-21 2009-02-10 Exxonmobil Chemical Patents Inc. Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking
US7235705B2 (en) 2004-05-21 2007-06-26 Exxonmobil Chemical Patents Inc. Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks
US7220887B2 (en) 2004-05-21 2007-05-22 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking hydrocarbon feedstock containing resid
US7767008B2 (en) 2004-12-10 2010-08-03 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus
US7481871B2 (en) 2004-12-10 2009-01-27 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus
US7674366B2 (en) 2005-07-08 2010-03-09 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US9409834B2 (en) 2005-07-19 2016-08-09 Exxonmobil Chemical Patents Inc. Low viscosity poly-alpha-olefins
US8105479B2 (en) 2009-06-18 2012-01-31 Exxonmobil Chemical Patents Inc. Process and apparatus for upgrading steam cracker tar-containing effluent using steam
US9365788B2 (en) 2011-10-10 2016-06-14 Exxonmobil Chemical Patents Inc. Process to produce improved poly alpha olefin compositions
EP2828367A1 (fr) 2012-03-22 2015-01-28 ExxonMobil Research and Engineering Company Nouvelle combinaison antioxydante et huiles de base synthétiques la contenant
US9777227B2 (en) 2014-04-30 2017-10-03 Exxonmobil Chemical Patents Inc. Upgrading hydrocarbon pyrolysis products
US9637694B2 (en) 2014-10-29 2017-05-02 Exxonmobil Chemical Patents Inc. Upgrading hydrocarbon pyrolysis products
WO2018111577A1 (fr) 2016-12-16 2018-06-21 Exxonmobil Chemical Patents Inc. Valorisation de goudron de pyrolyse
WO2018111574A1 (fr) 2016-12-16 2018-06-21 Exxonmobil Chemical Patents Inc. Prétraitement de goudron de pyrolyse
US20180170832A1 (en) 2016-12-20 2018-06-21 Exxonmobil Chemical Patents Inc. Process for Steam Cracking Hydrocarbons
WO2021204818A1 (fr) * 2020-04-07 2021-10-14 Total Research & Technology Feluy Valorisation d'huile à base de déchets plastiques en produits chimiques à valeur élevée par craquage catalytique direct

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
HAJEKOVA ET AL: "Copyrolysis of naphtha with polyalkene cracking products; the influence of polyalkene mixtures composition on product distribution", JOURNAL OF ANALYTICAL AND APPLIED PYROLYSIS, ELSEVIER BV, NL, vol. 79, no. 1-2, 19 April 2007 (2007-04-19), pages 196 - 204, XP022062362, ISSN: 0165-2370, DOI: 10.1016/J.JAAP.2006.12.022 *

Also Published As

Publication number Publication date
EP4652238A1 (fr) 2025-11-26
CN120731261A (zh) 2025-09-30

Similar Documents

Publication Publication Date Title
US20240368476A1 (en) Light Olefin Recovery from Plastic Waste Pyrolysis
CN1455809A (zh) 联合溶剂脱沥青和气化的沥青和树脂生产
US20230287276A1 (en) Plastic Waste Pyrolysis with Liquid Recycle
US20250354075A1 (en) Co-Processing Plastic Waste in Cokers for Jet Fuel Production
US20240191144A1 (en) Process and apparatus for cracking of thermally unstable feedstock
WO2007035210A1 (fr) Vapocraquage de pétrole brut à fort indice d’acidité (tan)
CN115698232A (zh) 含氮进料的烃热解
JP2024155735A (ja) 廃プラスチックからの精製炭化水素の製造方法および製造システム
WO2007005473A2 (fr) Vapocraquage de charges d'hydrocarbures partiellement dessalees
US8083930B2 (en) VPS tar separation
EP4652238A1 (fr) Processus de conversion de matériau plastique en oléfines
US20240247193A1 (en) Processes and Systems for Co-Processing a Hydrocarbon Feed and a Heavy Feed Containing a Plastic Material
US20230203386A1 (en) Hydrocarbon Pyrolysis of Advantaged Feeds
US20240247194A1 (en) Processes and Systems for Removing Deposits from an Integrated Plastic Pyrolysis Vessel and a Steam Cracking Furnace
US20250230365A1 (en) Contaminant Removal During Integrated Plastic Recycle
US20240360373A1 (en) Method and system for producing refined hydrocarbons and solid coke from waste plastics
WO2024129372A1 (fr) Co-traitement d'huile de pyrolyse par un dessaleur et un four de craquage avec séparateur vapeur-liquide intégré pour générer des produits circulaires
EP4544002A1 (fr) Procédés et systèmes de fractionnement d'un effluent de pyrolyse
WO2024206072A1 (fr) Procédé de cokéfaction et composition de coke contenant des métaux à l'état de trace

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 24705851

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 202480013699.7

Country of ref document: CN

WWE Wipo information: entry into national phase

Ref document number: 11202504724W

Country of ref document: SG

WWP Wipo information: published in national office

Ref document number: 11202504724W

Country of ref document: SG

WWP Wipo information: published in national office

Ref document number: 202480013699.7

Country of ref document: CN

WWP Wipo information: published in national office

Ref document number: 2024705851

Country of ref document: EP