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WO2025151334A1 - Procédés et appareils pour éliminer le monoxyde de carbone d'un flux d'éthylène - Google Patents

Procédés et appareils pour éliminer le monoxyde de carbone d'un flux d'éthylène

Info

Publication number
WO2025151334A1
WO2025151334A1 PCT/US2025/010198 US2025010198W WO2025151334A1 WO 2025151334 A1 WO2025151334 A1 WO 2025151334A1 US 2025010198 W US2025010198 W US 2025010198W WO 2025151334 A1 WO2025151334 A1 WO 2025151334A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
ethylene
carbon monoxide
zone
liquid
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
PCT/US2025/010198
Other languages
English (en)
Inventor
Vikrant DALAL
Eseoghene JERORO
James T. Wexler
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.)
Honeywell UOP LLC
Original Assignee
UOP LLC
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 UOP LLC filed Critical UOP LLC
Publication of WO2025151334A1 publication Critical patent/WO2025151334A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids

Definitions

  • One such exemplary process is the production of sustainable aviation fuel (SAF) from biorenewable source, such as biorenewable derived ethanol.
  • SAF sustainable aviation fuel
  • the conversion of ethanol feedstock to SAF is generally completed in four chemical processing steps: dehydration, oligomerization, hydrogenation, and fractionation.
  • dehydration oligomerization
  • hydrogenation hydrogenation
  • fractionation fractionation
  • carbon monoxide may negatively impact the oligomerization.
  • the process may include heating the liquid stream from the fractionation column with the ethylene stream before cooling the ethylene stream in the cooling zone.
  • the process may further include subcooling the refrigerant stream by transferring heat from the refrigerant stream to the gaseous portion from the vessel.
  • the ethylene stream may have a pressure of between 3,447 to 4, 137 kPa (500 to 600 psi(g)) and the liquid stream may have a pressure between 2,413 to 3,103 kPa (350 to 500 psi(g)).
  • the process may include cooling a process stream with the liquid stream.
  • the present invention may also be generally characterized as providing a process for producing jet range hydrocarbons from a biobased alcohol by: dehydrating a biobased alcohol stream in a dehydration zone comprising a reactor with a catalyst and being operated under conditions to provide a dehydrated effluent, the dehydrated effluent comprising ethylene and carbon monoxide; separating, from a feed stream comprising a portion of the dehydrated effluent, the carbon monoxide from the ethylene in a fractionation zone, the fractionation zone providing a bottoms stream comprising a carbon monoxide depleted ethylene stream and an overhead stream comprising carbon monoxide and ethylene; absorbing ethylene from a portion of the overhead stream in an absorption zone with an absorbing liquid stream to provide an enriched absorbing liquid stream comprising an increased level of ethylene and an ethylene depleted vapor stream comprising carbon monoxide; oligomerizing the carbon monoxide depleted liquid ethylene stream in an oligomerizing zone comprising a reactor with
  • the process may include separating the overhead stream in a vessel into a liquid portion and a gaseous portion, wherein the gaseous portion comprises the portion of the overhead stream from which ethylene is absorbed in the absorption zone, or cooling the overhead stream with a refrigerant stream in a cooling zone before separating the overhead stream; or both.
  • Figure 1 shows a process flow diagram according to one or more embodiments of the present invention.
  • Figure 2 shows a process flow diagram of a fractionation zone according to one or more embodiments of the present invention.
  • a biobased alcohol stream 10 is passed to a first reaction zone 12.
  • the biobased alcohol stream 10 is preferably, a biobased ethanol stream. Accordingly, the following detailed description will proceed with the embodiment that the feed stream 10 comprises a biobased ethanol stream however this is merely illustrative.
  • bio-based refers to organic materials in which the carbon comes from recently (on the order of centuries) fixated carbon dioxide present in the atmosphere using sunlight energy (photosynthesis). On land, this carbon dioxide is captured or fixated by plant life (e.g., agricultural crops or forestry materials). In the oceans, the carbon dioxide is captured or fixated by photosynthesizing bacteria or phytoplankton.
  • Biomass fermentation products typically include lower isoalkanols such as, for example, C2 to Cs isoalkanols obtained by contacting biomass with biocatalysts that facilitate conversion (by fermentation) of the biomass to isoalkanols.
  • the biomass feedstock for such fermentation processes can be any suitable fermentable feedstock known in the art, such as fermentable sugars derived from agricultural crops including sugarcane, com, etc.
  • suitable fermentable biomass feedstock can also be prepared by the hydrolysis of biomass, for example lignocellulosic biomass (e.g. wood, com stover, switchgrass, herbiage plants, ocean biomass, etc.), to form fermentable sugars.
  • the first reaction zone 12 is a dehydration zone comprising a reactor with a catalyst and being operated under conditions to provide a dehydrated effluent 14 which includes ethylene and carbon monoxide and which may also include hydrogen, carbon dioxide, methane, ethane, propane, propylene, butane, butenes, pentane, pentenes, and oxygenates such as diethyl ether, diethoxyethane, and ethyl acetate.
  • ethylene and carbon monoxide which may also include hydrogen, carbon dioxide, methane, ethane, propane, propylene, butane, butenes, pentane, pentenes, and oxygenates such as diethyl ether, diethoxyethane, and ethyl acetate.
  • Suitable catalyst may include alumina, modified alumina, silicoaluminate, modified silicoaluminate, or other catalysts known in the art.
  • the reactor may be operated at a temperature from 200° to 500° C (392° to 932° F).
  • the dehydration reactor may be operated at a pressure from 0 to 8,300 kPa (0 to 1, 204 psi(g)).
  • the dehydration reactor may be operated at a pressure from 0 to 3,500 kPa (0 to 508 psi(g)).
  • an insert gas such as nitrogen or steam may be introduced to the first reaction zone 12.
  • the dehydrated effluent 14 forms a feed stream for a fractionation zone 16.
  • the fractionation zone 16 is described in more detail below. However, generally, the fractionation zone 16 includes a fractionation column and provides a carbon monoxide depleted ethylene stream 22 and ethylene depleted vapor stream 20 comprising a significant portion of the carbon monoxide from the dehydrated effluent 14.
  • the carbon monoxide depleted ethylene stream 22 is passed to an oligomerizing zone 24 comprising a reactor with a catalyst and being operated under conditions to provide an oligomerized effluent 26.
  • the ethylene is converted into a mixture of heavier boiling hydrocarbons including jet range hydrocarbons via oligomerization by reacting the olefins using a catalyst under appropriate conditions.
  • the oligomerization zone 24 may, without limitation, be operated at a temperature from about 100 to about 300 °C (212 to 572 °F) and a pressure of from about 689 to about 6,895 kPa (100 to 1,000 psi(g)).
  • the oligomerization catalyst in the oligomerization zone 24 is not limited to any particular catalyst and may comprise any catalyst suitable for catalyzing conversion of the one or more biorenewable C2 to Cs olefins in the olefin stream to olefinic oligomers comprising heavier boiling C5+ hydrocarbons, including jet-range hydrocarbons.
  • the oligomerization catalyst may be any such catalyst known now or in the future. Exemplary oligomerization catalysts are described in U.S. Pat. Pub. No. 2023/0313048.
  • the oligomerized effluent 26 from the oligomerization zone 24 may be passed to a hydrogenation zone 28 having a hydrogenation reactor with a catalyst and being operated under conditions to provide a hydrogenated effluent 30.
  • Hydrogenation is typically performed using a conventional hydrogenation or hydro treating catalyst, which may include metallic catalysts containing, e.g., palladium, rhodium, nickel, ruthenium, platinum, rhenium, cobalt, molybdenum, or combinations thereof, and the supported versions thereof.
  • Catalyst supports can be any solid, inert substance including, but not limited to, oxides such as silica, alumina, titania, calcium carbonate, barium sulfate, and carbons.
  • the catalyst support can be in the form of powder, granules, pellets, or the like.
  • Hydrogenation suitably occurs at a temperature of between 38° to 260° C (100° to 500° F) and at a pressure of between about 689 to about 6,895 kPa (100 to 1,000 psi(g)).
  • a temperature of between 38° to 260° C 100° to 500° F
  • a pressure of between about 689 to about 6,895 kPa 100 to 1,000 psi(g)
  • Other process conditions known by those of ordinary skill in the art may be utilized.
  • the hydrogenated effluent 30 from the hydrogenation zone 28 will substantially comprise saturated hydrocarbons (i.e., paraffins).
  • the hydrogenated effluent 30 may be passed to a separation zone 32 having one or more columns configured and operated to separate the hydrogenated effluent 30 into one or more hydrocarbon streams 34, 36, 38 — one of which is a jet fuel hydrocarbon steam.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne des procédés et des appareils pour séparer le monoxyde de carbone de l'éthylène. L'éthylène peut être produit à partir d'alcool biosourcé. La séparation fait appel à une colonne de fractionnement qui produit une vapeur d'éthylène appauvrie en monoxyde de carbone et une vapeur de tête comprenant du monoxyde de carbone et de l'éthylène. L'éthylène provenant de la vapeur de tête peut être récupéré dans une zone d'absorption avec un liquide absorbant. Une zone de fractionnement d'oxygénat peut être utilisée pour éliminer les composés oxygénés du flux d'éthylène appauvri en monoxyde de carbone.
PCT/US2025/010198 2024-01-10 2025-01-03 Procédés et appareils pour éliminer le monoxyde de carbone d'un flux d'éthylène Pending WO2025151334A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202463619445P 2024-01-10 2024-01-10
US63/619,445 2024-01-10

Publications (1)

Publication Number Publication Date
WO2025151334A1 true WO2025151334A1 (fr) 2025-07-17

Family

ID=96387503

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2025/010198 Pending WO2025151334A1 (fr) 2024-01-10 2025-01-03 Procédés et appareils pour éliminer le monoxyde de carbone d'un flux d'éthylène

Country Status (1)

Country Link
WO (1) WO2025151334A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4525180A (en) * 1983-03-19 1985-06-25 Hidefumi Hirai Process for recovery of ethylene from gaseous mixture
US5220097A (en) * 1992-02-19 1993-06-15 Advanced Extraction Technologies, Inc. Front-end hydrogenation and absorption process for ethylene recovery
WO2013014003A1 (fr) * 2011-07-28 2013-01-31 Total Research & Technology Feluy Procédé pour éliminer des contaminants oxygénés d'un flux d'éthylène
WO2014091015A1 (fr) * 2012-12-13 2014-06-19 Total Research & Technology Feluy Procédé pour éliminer des constituants légers d'un flux d'éthylène
WO2023247188A1 (fr) * 2022-06-23 2023-12-28 Sabic Global Technologies B.V. Production d'éthylène par déshydrogénation oxydative d'éthane

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4525180A (en) * 1983-03-19 1985-06-25 Hidefumi Hirai Process for recovery of ethylene from gaseous mixture
US5220097A (en) * 1992-02-19 1993-06-15 Advanced Extraction Technologies, Inc. Front-end hydrogenation and absorption process for ethylene recovery
WO2013014003A1 (fr) * 2011-07-28 2013-01-31 Total Research & Technology Feluy Procédé pour éliminer des contaminants oxygénés d'un flux d'éthylène
WO2014091015A1 (fr) * 2012-12-13 2014-06-19 Total Research & Technology Feluy Procédé pour éliminer des constituants légers d'un flux d'éthylène
WO2023247188A1 (fr) * 2022-06-23 2023-12-28 Sabic Global Technologies B.V. Production d'éthylène par déshydrogénation oxydative d'éthane

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