EP4688254A2 - Déchloration de flux de liquide et de gaz d'un processus de pyrolyse de matières plastiques avec un adsorbant à base de nickel - Google Patents

Déchloration de flux de liquide et de gaz d'un processus de pyrolyse de matières plastiques avec un adsorbant à base de nickel

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Publication number
EP4688254A2
EP4688254A2 EP24782035.0A EP24782035A EP4688254A2 EP 4688254 A2 EP4688254 A2 EP 4688254A2 EP 24782035 A EP24782035 A EP 24782035A EP 4688254 A2 EP4688254 A2 EP 4688254A2
Authority
EP
European Patent Office
Prior art keywords
adsorbent
nickel
ppmw
alumina adsorbent
alumina
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP24782035.0A
Other languages
German (de)
English (en)
Inventor
Armin LANG DE OLIVEIRA
Bernard Reesink
Gisela Hieber
Dana Rehms Mooney
Garrett Dylan REHMS
Artem D. VITYUK
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.)
BASF Corp
Original Assignee
BASF Corp
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 BASF Corp filed Critical BASF Corp
Publication of EP4688254A2 publication Critical patent/EP4688254A2/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste

Definitions

  • hydroprocessing The only commercial solution accessible at scale that allows reduction of these impurities to 1-5 ppmw levels making these liquids drop-in substitute into naphtha crackers is hydroprocessing.
  • Hydroprocessing has been standardized in refining and does not require major process tune-ups if to be used for plastics pyrolysis liquids. The only major exception is chlorides/halogens.
  • Hydroprocessing catalysts perform hydrogenation of -N, -O, -S, and -Cl compounds which results in production of respective NH3, H2O, H2S, and HCL
  • there are issues with higher levels of chlorides in such units i.e.
  • a method of removing chlorides from a plastics pyrolysis stream comprising an initial chloride concentration of at least about 10 ppmw comprises: contacting the stream with an alumina adsorbent, the alumina adsorbent comprising precipitated nickel, wherein a final chloride concentration of the treated stream is less than about 10 ppmw.
  • the initial chloride concentration is from about 10 ppmw to about 45 ppmw.
  • the initial chloride concentration is from about 45 ppmw to about 250 ppmw.
  • the nickel is present from 50-70 wt% based on the total weight of the adsorbent.
  • the about 10 wt% to about 100 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • the about 25 wt% to about 45 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • the alumina adsorbent has a BET surface area of about 150 m 2 /g to about 200 m 2 /g.
  • the alumina adsorbent has a total pore volume from about 0.3 mL/g to about 6 mL/g.
  • the alumina adsorbent has a density of about 0.7 g/mL to about 1.0 g/mL.
  • the alumina adsorbent is in the form of extruded particles.
  • the extruded particles have an average extrudate length of about 3 mm to about 5 mm. In at least one embodiment, the extruded particles exhibit a side crush strength of greater than about 40 N.
  • a chlorides removal ratio is at least about 95% for a temperature of the pyrolysis stream from 200°C to 350°C.
  • the alumina adsorbent is regenerative.
  • the method further comprises subsequently contacting the alumina adsorbent with a regeneration stream to regenerate the alumina adsorbent.
  • the regeneration stream comprises hydrogen gas at a temperature of about 450°C to about 600°C.
  • the regeneration stream comprises oxygen gas at a temperature of about 250°C to about 350°C.
  • an adsorbent comprises: an alumina adsorbent; and precipitated nickel supported on the alumina adsorbent, wherein the nickel is present from 50 wt% to about 70 wt% based on the total weight of the adsorbent.
  • about 25 wt% to about 45 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • the alumina adsorbent has a BET surface area of about 150 m 2 /g to about 200 m 2 /g. In at least one embodiment, the alumina adsorbent has a total pore volume from about 0.3 mL/g to about 6 mL/g.
  • FIGURE is a plot of chlorides removal versus temperature for a sample prepared in accordance to the embodiments described herein tested against two comparative samples.
  • Embodiments of the present disclosure relate to processes and compositions for the efficient removal of chlorides from plastics pyrolysis streams (which may be liquid or gas streams).
  • plastics pyrolysis streams which may be liquid or gas streams.
  • certain embodiments utilize an adsorbent comprising nickel (e.g., precipitated nickel) for removing chlorides from a plastics pyrolysis stream (e.g., having an initial chloride concentration of greater than about 10 ppmw). It has been found that formulations based on nickel precipitation and/or impregnated on a support are active in removal of chlorides down to sub- ppmw levels.
  • the adsorbents described may utilize a porous support and one or more active metal components supported thereon.
  • Exemplary supports include metal oxides, metalloid oxides, activated carbons, and molecular sieves.
  • the support may include titanium oxide, ceria, alumina, silica, zirconia, magnesium oxide, zeolites, or combinations thereof.
  • supports include silica.
  • the support may include high surface area metal oxides.
  • the support may comprise aluminum oxide.
  • the support may comprise a mixture of titanium dioxide and aluminum oxide.
  • Metal oxide mixtures for example a mixture of titanium dioxide and aluminum oxide, may contain metal oxides in a weight/weight ratio of titanium dioxide to aluminum oxide of from any of about 9/1, about 8/1, about 7/1, about 6/1, about 5/1, about 4/1, about 3/1, about 2/1 or about 1/1 to any of about 1/2, about 1/3, about 1/4, about 1/5, aobut 1/6, about 1/7, about 1/8, or about 1/9.
  • the adsorbent comprises a high-pore volume support, such as high-pore volume alumina.
  • the alumina has an Na2O content of less than about 4000 ppmw.
  • the adsorbents described herein may be prepared by a variety of methods. For instance, a metal may be dispersed onto a support via an incipient-wetness technique. “Impregnated,” in general, means that the materials are “in” pores of the support. In at least one embodiment, the metal is precipitated onto the support. In at least one embodiment, the metal may be reduced after being dispersed or precipitated onto the support.
  • the adsorbent comprises nickel, for example, precipitated nickel or impregnated nickel. In at least one embodiment, the adsorbent comprises nickel from about 40 wt% to about 80 wt% based on the total weight of the adsorbent.
  • the nickel may be present at about 40 wt%, about 41 wt%, about 42 wt%, about 43 wt%, about 44 wt%, about 45 wt%, about 46 wt%, about 47 wt%, about 48 wt%, about 49 wt%, about 50 wt%, about 51 wt%, about 52 wt%, about 53 wt%, about 54 wt%, about 55 wt%, about 56 wt%, about 57 wt%, about 58 wt%, about 59 wt%, about 60 wt%, about 61 wt%, about 62 wt%, about 63 wt%, about 64 wt%, about 65 wt%, about 66 wt%, about 67 wt%, about 68 wt%, about 69 wt%, about 70 wt%, about 71 wt%, about 72 wt%, about
  • the nickel is fully/partially activated prior to treating a plastics pyrolysis stream.
  • the metal e.g., nickel
  • the metal is present in reduced form from about 10 wt% to about 100 wt%.
  • the nickel is present in reduced from at about 20 wt%, about 21 wt%, about 22 wt%, about 23 wt%, about 24 wt%, about 25 wt%, about 26 wt%, about 27 wt%, about 28 wt%, about 29 wt%, about 30 wt%, about 31 wt%, about 32 wt%, about 33 wt%, about 34 wt%, about 35 wt%, about 36 wt%, about 37 wt%, about 38 wt%, about 39 wt%, about 40 wt%, about 41 wt%, about 42 wt%, about 43 wt%, about 44 wt%, about 45 wt%, about 46 wt%, about 47 wt%, about 48 wt%, about 49 wt%, about 50 wt%, about 51 wt%, about 52 wt%, about 53 wt%, about 54
  • BET surface area is determined by the Brunauer-Emmett-Teller (BET) method according to DIN ISO 9277:2003-05 (which is a revised version of DIN 66131), and may be referred to as “BET surface area.”
  • the specific surface area is determined by a multipoint BET measurement in the relative pressure range from 0.05- 0.3 p/po.
  • the adsorbent has a BET surface area of about 100 m 2 /g, about 110 m 2 /g, about 120 m 2 /g, about 130 m 2 /g, about 140 m 2 /g, about 150 m 2 /g, about 160 m 2 /g, about 170 m 2 /g, about 180 m 2 /g, about 190 m 2 /g, about 200 m 2 /g, about 210 m 2 /g, about 220 m 2 /g, about 230 m 2 /g, about 240 m 2 /g, about 250 m 2 /g, greater than 250 m 2 /g, or in any range defined by and inclusive of these points (e.g., from about 150 m 2 /g to about 200 m 2 /g).
  • Pore volume and average pore radius are determined by the Barret- Joyner-Halenda (BJH) method.
  • BJH Barret- Joyner-Halenda
  • Mercury porosimetry analysis can be used to characterize porosity. Mercury porosimetry applies controlled pressure to a sample immersed in mercury. External pressure is applied for the mercury to penetrate into the voids/pores of the material. The amount of pressure required to intrude into the voids/pores is inversely proportional to the size of the voids/pores.
  • a mercury porosimeter generates volume and pore size distributions from the pressure versus intrusion data generated by the instrument using the Washburn equation: > — g cos q
  • porous silica microspheres containing voids/pores with an average size of about 165 nm can have an average porosity of about 0.8.
  • the alumina adsorbent has a total volume of about 0.1 mL/g, about 0.2 mL/g, about 0.3 mL/g, about 0.4 mL/g, about 0.5 mL/g, about 0.6 mL/g, about 0.7 mL/g, about 0.8 mL/g, about 0.9 mL/g, about 1.0 mL/g, about 1.5 mL/g, 2.0 mL/g, about 2.5 mL/g, 3.0 mL/g, about 3.5 mL/g, 4.0 mL/g, about 4.5 mL/g, 5.0 mL/g, about 5.5 mL/g, about 6.0 mL/g, greater than about 6.0 mL/g, or in any range defined by and inclusive of these points (e.g., from about 0.3 mL/g to about 6 mL/g).
  • the adsorbent has a density of about 0.5 g/mL, about 0.6 g/mL, about 0.7 g/mL, about 0.8 g/mL, about 0.9 g/mL, about 1.0 g/mL, about 1.1 g/mL, about 1.2 g/mL, about 1.3 g/mL, about 1.4 g/mL, about 1.5 g/mL, or in any range defined by or inclusive of these points (e.g., about 0.7 g/mL to about 1.0 g/mL).
  • the suitable components may be present in the adsorbent compositions in a bulk form, meaning in a continuous form that is in general not interrupted by other materials.
  • a bulk form may contain substantially no other materials.
  • the adsorbent compositions may be in any suitable final form, for instance, tablets, extrudates, pellets, rods, moldings or monoliths, etc., in various shapes and sizes.
  • an adsorbent e.g., an alumina adsorbent having precipitated or impregnated nickel
  • an extruded material such as extruded particles.
  • the extruded particles are elongated and may have an average extrudate length (i.e., an average largest dimension) of about 1 mm, about 2 mm, about 3 mm, about 4 mm, about 5 mm, about 6 mm, or in any range defined by and inclusive of these points (e.g., from about 3 mm to about 5 mm).
  • the extruded particles exhibit a side crush strength of greater than about 10 N, greater than about 20 N, greater than about 30 N, greater than about 40 N, greater than about 50 N, greater than about 60 N, greater than about 70 N, greater than about 80 N, greater than about 90 N, or greater than about 100 N.
  • the adsorbents described herein may be suitable for removing chlorides and/or other components from feed streams, such as plastics pyrolysis streams.
  • chlorides refers to chlorine-containing compounds that may include, but not limited to, chloroalkanes, chloroalkenes, chlorooxygenates, chloronaphthenes, and chloroaromatics.
  • Streams suitable for treatment by the adsorbents described herein may include a chlorides content of greater than about 10 ppmw, up to about 500 ppmw (e.g., about 10 ppmw to about 45 ppmw, or about 100 ppmw to about 250 ppmw), or greater.
  • the adsorbent exhibits a chlorides removal ratio of at least about 90%, at least about 91%, at least about 92%, at least about 93%, at least about 94%, at least about 95%, at least about 96%, at least about 97%, at least about 98%, or at least about 99% when contacted with a pyrolysis liquid stream (e.g., having a chlorides content of greater than about 80 ppmw) at a temperature from about 200°C to 350°C.
  • a pyrolysis liquid stream e.g., having a chlorides content of greater than about 80 ppmw
  • the adsorbent is regenerative (i.e., the adsorbent is capable of being regenerated to restore its activity to or near its activity prior to use).
  • the adsorbent can be regenerated by treating the adsorbent with a regeneration stream.
  • the regeneration stream is at a temperature of about 450°C to about 600°C and comprises hydrogen gas.
  • the regeneration stream is at a temperature of about 250°C to about 350°C and comprises oxygen gas.
  • Weight percent if not otherwise indicated, is based on an entire composition free of any volatiles, that is, based on dry solids content.
  • Embodiment 1 A method of removing chlorides from a plastics pyrolysis stream comprising an initial chloride concentration of at least about 10 ppmw, the method comprising: contacting the stream with an alumina adsorbent, the alumina adsorbent comprising precipitated nickel, wherein a final chloride concentration of the treated stream is less than about 10 ppmw.
  • Embodiment 2 The method of Embodiment 1, wherein the initial chloride concentration is from about 10 ppmw to about 45 ppmw.
  • Embodiment 3 The method of Embodiment 1, wherein the initial chloride concentration is from about 45 ppmw to about 250 ppmw.
  • Embodiment 4 The method of any of the preceding Embodiments, wherein the nickel is present from 50-70 wt% based on the total weight of the adsorbent.
  • Embodiment 5 The method of Embodiment 4, wherein the about 10 wt% to about 100 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • Embodiment 6 The method of Embodiment 4, wherein the about 25 wt% to about 45 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • Embodiment 7 The method of any of the preceding Embodiments, wherein the alumina adsorbent has a BET surface area of about 150 m 2 /g to about 200 m 2 /g.
  • Embodiment 8 The method of any of the preceding Embodiments, wherein the alumina adsorbent has a total pore volume from about 0.3 mL/g to about 6 mL/g.
  • Embodiment 9 The method of any of the preceding Embodiments, wherein the alumina adsorbent has a density of about 0.7 g/mL to about 1.0 g/mL.
  • Embodiment 10 The method of any of the preceding Embodiments, wherein the alumina adsorbent is in the form of extruded particles.
  • Embodiment 11 The method of Embodiment 10, wherein the extruded particles have an average extrudate length of about 3 mm to about 5 mm.
  • Embodiment 12 The method of either Embodiment 10 or Embodiment 11, wherein the extruded particles exhibit a side crush strength of greater than about 40 N.
  • Embodiment 13 The method of any of the preceding Embodiments, wherein a chlorides removal ratio is at least about 95% for a temperature of the pyrolysis stream from 200°C to 350°C.
  • Embodiment 14 The method of any of the preceding Embodiments, wherein the alumina adsorbent is regenerative.
  • Embodiment 15 The method of Embodiment 14, further comprising: subsequently contacting the alumina adsorbent with a regeneration stream to regenerate the alumina adsorbent.
  • Embodiment 16 The method of Embodiment 15, wherein the regeneration stream comprises hydrogen gas at a temperature of about 450°C to about 600°C.
  • Embodiment 17 The method of Embodiment 15, wherein the regeneration stream comprises oxygen gas at a temperature of about 250°C to about 350°C.
  • Embodiment 18 An adsorbent comprising: an alumina adsorbent; and precipitated nickel supported on the alumina adsorbent, wherein the nickel is present from 50-70 wt% based on the total weight of the adsorbent.
  • Embodiment 19 The adsorbent of Embodiment 18, wherein about 25 wt% to about 45 wt% of the nickel is present in reduced form based on the total amount of nickel present.
  • Embodiment 20 The adsorbent of either Embodiment 18 or Embodiment 19, wherein the alumina adsorbent has a BET surface area of about 150 m 2 /g to about 200 m 2 /g, and wherein the alumina adsorbent has a total pore volume from about 0.3 mL/g to about 6 mL/g.
  • sample comprising reduced nickel (about 60 wt% total nickel, and about 30 wt% to about 35 wt% of total nickel being in reduced form) on a high-pore volume alumina adsorbent (BET surface area of about 170 m 2 /g to about 200 m 2 /g) was tested against two comparative samples: an alumina adsorbent with 4-5 wt% Na2O (“Guard A”), and unreduced NiO impregnated on alumina (“Guard B”).
  • Guide A alumina adsorbent with 4-5 wt% Na2O
  • Guard B unreduced NiO impregnated on alumina
  • the pyrolysis oil had a chlorides concentration at the inlet of about 80 ppmw, and was evaluated across temperatures from 200-330 °C at a pressure of 50 barg.
  • the Sample exhibited nearly 100% chlorides removal over the range of temperatures, demonstrating significantly improved performance over the comparative examples at higher temperatures.
  • X includes A or B is intended to mean any of the natural inclusive permutations. That is, if X includes A; X includes B; or X includes both A and B, then “X includes A or B” is satisfied under any of the foregoing instances.
  • adsorbent composition that is substantially free of lead may refer to an adsorbent composition for which lead is below a detectable limit, or its presence has a negligible effect on the performance of the adsorbent.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

L'invention concerne des procédés et des matériaux pour la déchloration de flux de liquide et de gaz. Dans au moins un mode de réalisation, un procédé comprend la mise en contact d'un flux de pyrolyse de matières plastiques avec un adsorbant d'alumine, l'adsorbant d'alumine comprenant du nickel précipité.
EP24782035.0A 2023-03-30 2024-03-29 Déchloration de flux de liquide et de gaz d'un processus de pyrolyse de matières plastiques avec un adsorbant à base de nickel Pending EP4688254A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202363455743P 2023-03-30 2023-03-30
PCT/US2024/022245 WO2024206832A2 (fr) 2023-03-30 2024-03-29 Déchloration de flux de liquide et de gaz d'un processus de pyrolyse de matières plastiques avec un adsorbant à base de nickel

Publications (1)

Publication Number Publication Date
EP4688254A2 true EP4688254A2 (fr) 2026-02-11

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP24782035.0A Pending EP4688254A2 (fr) 2023-03-30 2024-03-29 Déchloration de flux de liquide et de gaz d'un processus de pyrolyse de matières plastiques avec un adsorbant à base de nickel

Country Status (2)

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EP (1) EP4688254A2 (fr)
WO (1) WO2024206832A2 (fr)

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5863852A (en) * 1996-10-10 1999-01-26 Air Products And Chemicals, Inc. Regeneration of adsorbent beds
US8969422B2 (en) * 2010-03-13 2015-03-03 Quzhou City Guangyuan Domestic Garbage Liquefy Technology Institute Method, system and equipment for gasification-liquefaction disposal of municipal solid waste
US20140330057A1 (en) * 2013-05-02 2014-11-06 Shell Oil Company Process for converting a biomass material
JP6824981B2 (ja) * 2015-11-13 2021-02-03 サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ 炭化水素供給物流の塩化物含有量を減少させるための触媒プロセス
EP3516012B1 (fr) * 2016-09-22 2021-01-06 SABIC Global Technologies B.V. Configuration de procédé intégrée et dispositif impliquant les étapes de pyrolyse, d'hydrocraquage, d'hydrodésalkylation et de craquage à la vapeur
US10975313B2 (en) * 2017-01-05 2021-04-13 Sabic Global Technologies B.V. Conversion of waste plastic through pyrolysis to high value products like benzene and xylenes
US12234412B2 (en) * 2019-05-14 2025-02-25 Anellotech, Inc. Olefin and aromatics production by the catalytic pyrolysis of polymers

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WO2024206832A2 (fr) 2024-10-03

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