WO2012135111A2 - Récupération de composés aromatiques par extraction par distillation - Google Patents

Récupération de composés aromatiques par extraction par distillation Download PDF

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Publication number
WO2012135111A2
WO2012135111A2 PCT/US2012/030550 US2012030550W WO2012135111A2 WO 2012135111 A2 WO2012135111 A2 WO 2012135111A2 US 2012030550 W US2012030550 W US 2012030550W WO 2012135111 A2 WO2012135111 A2 WO 2012135111A2
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WO
WIPO (PCT)
Prior art keywords
solvent
hydrocarbons
polar
column
contaminated
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/US2012/030550
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English (en)
Other versions
WO2012135111A3 (fr
Inventor
Robert J. L. NOE
Bruce R. Beadle
Lawrence E. Sullivan
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
Priority claimed from US13/428,731 external-priority patent/US8552247B2/en
Application filed by UOP LLC filed Critical UOP LLC
Publication of WO2012135111A2 publication Critical patent/WO2012135111A2/fr
Publication of WO2012135111A3 publication Critical patent/WO2012135111A3/fr
Anticipated expiration legal-status Critical
Ceased 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/16—Oxygen-containing compounds
    • 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
    • C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
    • C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/27—Organic compounds not provided for in a single one of groups C10G21/14 - C10G21/26
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents
    • 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
    • C10G2400/30—Aromatics

Definitions

  • the present invention relates to the recovery of aromatic hydrocarbons from a stream containing a mixture of aromatic and aliphatic hydrocarbons. More specifically, the invention relates to an extractive distillation process for the recovery of aromatics and a method for purifying the extractive-distillation solvent for use in a closed solvent loop.
  • Extractive distillation is a key separation method used in chemical processing, especially for the recovery of aromatics from hydrocarbon mixtures.
  • a key aspect of extractive distillation is that a separating agent, a solvent with a high boiling point, is added to a component mixture for separation which increases relative volatility when the components have similar or close boiling points.
  • Aromatic hydrocarbons can be recovered from mixtures containing aromatic and non-aromatic hydrocarbons by liquid-liquid extraction.
  • suitable feedstocks for extraction are mixtures containing benzene, toluene and xylene derived from the catalytic reforming of naphtha or from the hydrogenation of raw pyrolysis gasoline byproduct from olefin production.
  • Extractive distillation is an alternative aromatics-recovery process which typically is applied to lighter hydrocarbon fractions and comprises an extractive-distillation column and a solvent-recovery column.
  • a nonvolatile solvent passes to an upper section and the hydrocarbon fraction is introduced to a middle section of the extractive-distillation column.
  • the solvent descends through the column, it preferentially extracts the polar components (aromatics) to form a rich solvent while the non-polar component vapor comprising non-polar components ascends to the top of the column.
  • Overhead vapor is condensed, with a portion of the condensate being recycled to the top section of the extractive-distillation column as reflux while a net portion is withdrawn as a raffinate product.
  • the rich solvent from the bottom of the extractive-distillation column comprising the solvent and the polar components, is fed into a solvent recovery column to recover aromatics as an overhead product along with reflux to the recovery column.
  • Bottoms from the solvent-recovery column are lean solvent, free of the feed components, which is recycled to the upper portion of the extractive-distillation column as the extractive solvent.
  • Extractive distillation requires less equipment, for example two instead of four separation columns, and has a lower energy requirement than solvent extraction, but the application of this process is restricted by requiring a narrower feedstock boiling range than liquid-liquid extraction.
  • the feedstock to extractive distillation normally is obtained by fractionation of a wider-range hydrocarbon fraction. Extractive distillation most often is targeted to the recovery of benzene from a fraction rich in C 6 and C 7 hydrocarbons, but small amounts of heavy hydrocarbons remain even in such light fractions. These heavy hydrocarbons tend to remain with the rich solvent at the bottom of the extractive-distillation column due to their high boiling points, and accumulate in the solvent due to the solvent being circulated within a closed loop, with consequent inefficient column and process operation.
  • a broad aspect of the present invention is a method for recovering a substantially hydrocarbon-free, water-soluble polar-hydrocarbon-selective solvent from a solvent-rich stream comprising hydrocarbons and heavy waste products, the method comprising (a) introducing a hydrocarbon feedstock comprising polar and non-polar hydrocarbons into an intermediate section of an extractive-distillation column, introducing a circulating polar solvent into an upper section of the column, recovering a raffinate product comprising non- polar hydrocarbons and water overhead from the column, and removing a rich solvent comprising polar solvent and polar hydrocarbons from the bottom of the column; (b) introducing the rich solvent into a rich-solvent fractionator, recovering an extract product comprising polar hydrocarbons overhead from the fractionator and a contaminated solvent from the bottom of the column; (c) dividing the contaminated solvent into a first portion and a second portion and directing the first portion to a first solvent-purification vessel containing a solid adsorbent
  • step (e) subjecting the first solvent-purification vessel of step (c) containing contaminated adsorbent to the method of step (d) and the second solvent-purification vessel of step (d) to the method of step (c); and (f) combining the second portion of contaminated solvent and purified solvent to provide the circulating polar solvent.
  • a more specific aspect of the invention is a method for recovering a substantially hydrocarbon-free, water-soluble polar-hydrocarbon-selective solvent from a solvent-rich stream comprising hydrocarbons and heavy waste products, the method comprising (a) introducing a hydrocarbon feedstock comprising aromatic and non-aromatic hydrocarbons into an intermediate section of an extractive-distillation column, introducing a circulating polar solvent into an upper section of the column, recovering a raffinate product comprising non-aromatic hydrocarbons and water overhead from the column, and removing a rich solvent comprising polar solvent and aromatic hydrocarbons from the bottom of the column; (b) introducing the rich solvent into a rich-solvent fractionator, recovering an extract product comprising aromatic hydrocarbons overhead from the fractionator and a contaminated solvent from the bottom of the column; (c) dividing the contaminated solvent into a first portion and a second portion and directing the first portion to a first solvent-purification vessel containing a solid adsorbent
  • a yet more specific aspect of the invention is a method for recovering a
  • substantially hydrocarbon-free, water-soluble polar-hydrocarbon-selective solvent from a solvent-rich stream comprising hydrocarbons and heavy waste products comprising (a) introducing a hydrocarbon feedstock comprising benzene and non-aromatic hydrocarbons into an intermediate section of an extractive-distillation column, introducing a circulating polar solvent into an upper section of the column, recovering a raffinate product comprising non-aromatic hydrocarbons and water overhead from the column, and removing a rich solvent comprising polar solvent and benzene from the bottom of the column; (b) introducing the rich solvent into a rich-solvent fractionator, recovering an extract product comprising benzene overhead from the fractionator and a contaminated solvent from the bottom of the column; (c) dividing the contaminated solvent into a first portion and a second portion and directing the first portion to a first solvent-purification vessel containing a solid adsorbent to yield a purified solvent and a contaminated adsorb
  • FIG. 1 The Figure is a schematic illustration of an extractive-distillation process incorporating the solvent-purification step of the invention.
  • This invention provides an improved extractive-distillation process for recovering polar hydrocarbons from non-polar hydrocarbons, such as aromatics from non-aromatics, naphthenes from paraffins and isoparaffins, or olefins from paraffins and isoparaffins, in feed mixtures containing at least a measurable amount of heavier hydrocarbons which are extracted from petroleum streams.
  • this invention relates to an improved extractive-distillation process for recovering aromatic hydrocarbons including benzene, toluene, and xylenes (BTX aromatics) from the C 6 -C 8 petroleum streams containing at least a measurable amount of Cg+ hydrocarbons.
  • this invention relates to an improved extractive-distillation process for recovering mainly benzene and toluene from the C 6 -C 7 petroleum streams containing at least a measurable amount of Ce+ hydrocarbons.
  • this invention is directed toward the regeneration, recovery and purification of the extractive-distillation solvent utilized to recover pure aromatic
  • hydrocarbons from the hydrocarbon stream containing at least a measurable amount of hydrocarbons heavier than intend feedstock are hydrocarbons from the hydrocarbon stream containing at least a measurable amount of hydrocarbons heavier than intend feedstock.
  • a feed containing polar and non-polar hydrocarbons is introduced into a middle portion of an extractive-distillation column and a solvent-rich stream is fed into an upper portion of the extractive-distillation column as the selective solvent feed.
  • a water-containing non-polar-hydrocarbon-rich stream is recovered from the upper portion of the extractive-distillation column.
  • a first solvent-rich stream containing the aqueous solvent and the polar hydrocarbons is recovered from a bottom portion of the extractive-distillation column.
  • the first solvent-rich stream is introduced into a middle portion of a solvent-recovery column and a polar hydrocarbon-rich stream, substantially free from said aqueous solvent and said non-polar hydrocarbons is recovered from an upper portion of the solvent-recovery column.
  • a second solvent-rich stream is removed from a bottom portion of the solvent- recovery column and a greater portion of the second solvent-rich stream is fed into the upper portion of the extractive-distillation column.
  • a lesser fraction of the second solvent-rich stream is passed into a first solvent-purification vessel containing an adsorbent suitable for removing hydrocarbons and other contaminants from the solvent, and purified solvent from this vessel is combined with the greater portion of the solvent-rich stream to the upper portion of the extractive-distillation column.
  • a portion of the raffinate product is sent to a second solvent-purification vessel containing adsorbent contaminated by hydrocarbons and other contaminants and removes the contaminants, joining the raffinate product as feed to the solvent-regeneration column. Water and any hydrocarbons and other compounds having boiling points lower than or equal to that of said aqueous solvent is recovered from the upper portion of the solvent regeneration zone.
  • a hydrocarbon feed containing a mixture of aromatic and non- aromatic hydrocarbons is fed via conduit 1 to a middle section of an extractive-distillation column 10, while a lean solvent is fed via conduit 2 to near the top of the extractive- distillation column below the entry point of overhead reflux 3.
  • Non-aromatics vapor exiting the top of the extractive-distillation column through conduit 4 is condensed via condenser 5 and transferred to an overhead receiver 6, which serves to effect a phase separation between the non-aromatic raffinate and the water phase.
  • a first portion of the non-aromatic raffinate is recycled to a top section of the extractive-distillation column as reflux via conduit 3, while a second portion of the non-aromatic raffinate is withdrawn as a raffinate product through conduit 7.
  • the water phase in conduit 8 is returned to the extractive distillation column 10.
  • the rich solvent stream containing the solvent, aromatic hydrocarbons, and measurable heavy hydrocarbons is withdrawn from the bottom section of the extractive- distillation column and heated in a reboiler 1 1 and recycled to the bottom section of the extractive-distillation column via conduit 12 to generate vapor to the column.
  • the rich solvent from the bottom of the extractive distillation column 10 is fed to a middle section of the solvent-recovery column 20 through conduit 13.
  • An aromatic concentrate containing water and being substantially free of solvent and non-aromatic hydrocarbons is withdrawn from solvent-recovery column 20 through conduit 21 as an overhead vapor stream, condensed in condenser 22, and introduced into an overhead receiver 23.
  • the overhead receiver serves to effect a phase separation between the aromatic-hydrocarbon phase and the water phase 24.
  • a first portion of the aromatic hydrocarbon phase is recycled to a top section of the solvent-recovery column as the reflux via conduit 25, while a second portion of the aromatic hydrocarbon phase is withdrawn as the aromatic hydrocarbon product through conduit 26.
  • the water phase is transferred through conduit 24 preferably to a steam generator to form stripping steam for the solvent-recovery column.
  • the overhead receiver 23 is connected to a vacuum source to generate sub-atmospheric condition in the solvent-recovery column.
  • Small amounts of olefinic hydrocarbons are more concentrated in the heavy hydrocarbons fraction, and the load of a clay tower in an aromatics complex for olefinic hydrocarbons removal from the aromatic product can be significantly reduced by keeping the heavy hydrocarbons at the bottom of the solvent-recovery column with the lean solvent; the olefinic as well as heavy aromatic hydrocarbons can be removed from the closed solvent loop by the purification step of this invention.
  • a portion of the lean solvent in conduit 27 is heated in a reboiler 28 and recycled to the bottom section of the solvent-recovery column via conduit 29 to generate vapor to the column, while the remaining portion of the contaminated lean solvent in conduit 30 passes to the solvent-purification section.
  • the solvent-purification section comprises two or more vessels which are alternatively in adsorption and regeneration mode. Part of the lean solvent may bypass the solvent-purification section as lean solvent to extractive distillation in conduit 2.
  • a first portion of contaminated solvent to be purified is directed via conduit 31 to one or more first solvent-purification vessels in vessel 33 containing a solid adsorbent, which adsorbs contaminants from the solvent to yield a purified solvent in conduit 34 and a contaminated adsorbent in vessel 33.
  • a second portion of contaminated solvent in conduit 32 is combined with purified solvent to provide a circulating solvent to extractive distillation in conduit 2.
  • a portion of the water phase in conduit 24 is sent via conduit 35 to one or more vessels 36 which have received contaminated solvent and contain contaminated adsorbent to yield contaminated solid adsorbent essentially free of solvent in vessel 36 and water and solvent in conduit 37.
  • a portion of the raffinate of stream 7 is used to remove the heavy contaminant from the adsorbent in stream 38 and remove contaminant from the process in conduit 39
  • the water-soluble, aqueous solvent is selected from the list comprising sulfolane, alkyl-sulfolane, N-formyl morpholine, N-methyl pyrrolidone, tetraethylene glycol, triethylene glycol, diethylene glycol, and mixtures thereof.
  • the water-soluble solvent is aqueous sulfolane
  • the water-soluble solvent is aqueous N-formyl morpholine
  • the water-soluble solvent is aqueous N- methylpyrrolidone
  • the water-soluble solvent is aqueous tetraethylene glycol.
  • the solvent consists essentially of sulfolane.
  • Degradation of the sulfolane solvent occurs at temperatures above 200°C in an inert atmosphere and increases significantly in oxygen-containing atmosphere, where air leaks through the extractive-distillation process equipment which operates in a vacuum.
  • the primary products from degradation of sulfolane are sulfur dioxide and oxygen-containing organic compounds, such as aldehydes, organosulfonic acids, carboxylic acids, etc., which are removed from the solvent using the process of the invention.
  • a variety of adsorbents are suitable for contaminant removal in the solvent- purification vessels.
  • Polymeric adsorbents such as those used for oil recovery are suitable adsorbents.
  • Other suitable sorbents include alumina, silica, silica-alumina, zeolitic and non- zeolitic molecular sieves and activated carbon.
  • the purified organic solvent fluid flowing through the fluid flow pathway may be recirculated such that it undergoes multiple passes through the solvent-purification vessels.
  • the purification zone typically is operated at a temperature of 0° to 100° C. and a pressure of 1 to 100 atmospheres.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de récupération d'hydrocarbures polaires à partir d'hydrocarbures non polaires, comme des composés aromatiques à partir de composés non aromatiques, des naphtènes à partir de paraffines et d'isoparaffines ou des oléfines à partir de paraffines et d'isoparaffines, dans des mélanges d'alimentation contenant au moins une quantité mesurable d'hydrocarbures plus lourds. L'invention décrit un procédé amélioré d'extraction par distillation (extraction-distillation) permettant de récupérer des hydrocarbures aromatiques, tels que le benzène, le toluène et les xylènes, à partir d'hydrocarbures (C9+) lourds. L'invention concerne également un procédé amélioré d'extraction par distillation permettant de récupérer principalement du benzène et du toluène à partir de courants de pétrole en C6-C7 contenant au moins une quantité mesurable d'hydrocarbures en C8+. En outre, l'invention concerne la régénération et la récupération du solvant d'extraction-distillation utilisée pour récupérer et purifier les hydrocarbures aromatiques à partir du courant de pétrole contenant au moins une quantité mesurable d'hydrocarbures plus lourds que le produit attendu.
PCT/US2012/030550 2011-03-31 2012-03-26 Récupération de composés aromatiques par extraction par distillation Ceased WO2012135111A2 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201161470059P 2011-03-31 2011-03-31
US61/470,059 2011-03-31
US13/428,731 US8552247B2 (en) 2011-03-31 2012-03-23 Aromatics recovery by extractive distillation
US13/428,731 2012-03-23

Publications (2)

Publication Number Publication Date
WO2012135111A2 true WO2012135111A2 (fr) 2012-10-04
WO2012135111A3 WO2012135111A3 (fr) 2013-01-03

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AR (1) AR085777A1 (fr)
TW (1) TWI464146B (fr)
WO (1) WO2012135111A2 (fr)

Cited By (13)

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Publication number Priority date Publication date Assignee Title
WO2013126131A3 (fr) * 2012-02-26 2013-11-14 Amt International, Inc. Régénération de solvants sélectifs pour des procédés d'extraction
WO2015000840A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé pour le craquage d'une charge d'hydrocarbures dans une unité de vapocraquage
WO2015000850A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé et installation pour la conversion du pétrole brut en produits pétrochimiques ayant un rendement amélioré en btx
WO2015000841A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé d'enrichissement de résidus lourds de raffinerie en produits pétrochimiques
WO2015000844A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé de craquage d'une matière première hydrocarbonée dans une unité de craquage à vapeur
WO2015000843A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé pour la production d'oléfines légères et de composés aromatiques à partir d'une charge de départ d'hydrocarbures
EP3040324A1 (fr) * 2014-12-30 2016-07-06 Shell Internationale Research Maatschappij B.V. Procédé pour la conversion de composés oxygénés en produits aromatiques
US9856425B2 (en) 2013-07-02 2018-01-02 Saudi Basic Industries Corporation Method of producing aromatics and light olefins from a hydrocarbon feedstock
CN112546675A (zh) * 2020-12-28 2021-03-26 大连福佳·大化石油化工有限公司 床层漏剂的吸附塔汽提改进结构
US11072748B2 (en) * 2019-12-09 2021-07-27 Saudi Arabian Oil Company Selective reforming process to produce gasoline blending components and aromatics
WO2022026134A1 (fr) 2020-07-31 2022-02-03 Exxonmobil Chemical Patents Inc. Procédés d'extraction et/ou de séparation d'hydrocarbures utilisant un séparateur à membrane
WO2022079059A1 (fr) * 2020-10-16 2022-04-21 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
WO2022186974A1 (fr) 2021-03-05 2022-09-09 Exxonmobil Chemical Patents Inc. Procédés d'extraction d'hydrocarbures utilisant un lit de nettoyage

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US9221729B1 (en) * 2015-02-23 2015-12-29 Allnew Chemical Technology Company Extractive distillation for aromatics recovery
CN110604967A (zh) * 2019-10-15 2019-12-24 北京宝晨能源工程技术有限公司 一种环丁砜再生装置及方法

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US7666299B2 (en) * 2007-08-10 2010-02-23 Amt International, Inc. Extractive distillation process for recovering aromatics from petroleum streams
US7871514B2 (en) * 2007-08-10 2011-01-18 Cpc Corporation, Taiwan Extractive distillation processes using water-soluble extractive solvents

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US9440947B2 (en) 2012-02-26 2016-09-13 Amt International, Inc. Regeneration of selective solvents for extractive processes
WO2013126131A3 (fr) * 2012-02-26 2013-11-14 Amt International, Inc. Régénération de solvants sélectifs pour des procédés d'extraction
US10465131B2 (en) 2013-07-02 2019-11-05 Saudi Basic Industries Corporation Process for the production of light olefins and aromatics from a hydrocarbon feedstock
US10822558B2 (en) 2013-07-02 2020-11-03 Saudi Basic Industries Corporation Method for cracking a hydrocarbon feedstock in a steam cracker unit
WO2015000844A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé de craquage d'une matière première hydrocarbonée dans une unité de craquage à vapeur
WO2015000843A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé pour la production d'oléfines légères et de composés aromatiques à partir d'une charge de départ d'hydrocarbures
US11072750B2 (en) 2013-07-02 2021-07-27 Saudi Basic Industries Corporation Process for upgrading refinery heavy residues to petrochemicals
WO2015000850A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé et installation pour la conversion du pétrole brut en produits pétrochimiques ayant un rendement amélioré en btx
US9856425B2 (en) 2013-07-02 2018-01-02 Saudi Basic Industries Corporation Method of producing aromatics and light olefins from a hydrocarbon feedstock
US9862898B2 (en) 2013-07-02 2018-01-09 Saudi Basic Industries Corporation Process and installation for the conversion of crude oil to petrochemicals having an improved BTX yield
WO2015000840A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé pour le craquage d'une charge d'hydrocarbures dans une unité de vapocraquage
US10526553B2 (en) 2013-07-02 2020-01-07 Saudi Basic Industries Corporation Method for cracking a hydrocarbon feedstock in a steam cracker unit
WO2015000841A1 (fr) 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Procédé d'enrichissement de résidus lourds de raffinerie en produits pétrochimiques
US11046900B2 (en) 2013-07-02 2021-06-29 Saudi Basic Industries Corporation Process for upgrading refinery heavy residues to petrochemicals
EP3040324A1 (fr) * 2014-12-30 2016-07-06 Shell Internationale Research Maatschappij B.V. Procédé pour la conversion de composés oxygénés en produits aromatiques
US11072748B2 (en) * 2019-12-09 2021-07-27 Saudi Arabian Oil Company Selective reforming process to produce gasoline blending components and aromatics
US12145908B2 (en) 2020-07-31 2024-11-19 ExxonMobil Engineering & Technology Company Hydrocarbon extraction and/or separation processes utilizing a membrane separator
WO2022026134A1 (fr) 2020-07-31 2022-02-03 Exxonmobil Chemical Patents Inc. Procédés d'extraction et/ou de séparation d'hydrocarbures utilisant un séparateur à membrane
WO2022079059A1 (fr) * 2020-10-16 2022-04-21 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
CN112546675B (zh) * 2020-12-28 2023-10-13 大连福佳·大化石油化工有限公司 床层漏剂的吸附塔汽提改进结构
CN112546675A (zh) * 2020-12-28 2021-03-26 大连福佳·大化石油化工有限公司 床层漏剂的吸附塔汽提改进结构
WO2022186974A1 (fr) 2021-03-05 2022-09-09 Exxonmobil Chemical Patents Inc. Procédés d'extraction d'hydrocarbures utilisant un lit de nettoyage
CN117015591A (zh) * 2021-03-05 2023-11-07 埃克森美孚化学专利公司 利用清洁床的烃萃取方法

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