US3435087A - Recovery of aromatics - Google Patents

Recovery of aromatics Download PDF

Info

Publication number
US3435087A
US3435087A US499974A US3435087DA US3435087A US 3435087 A US3435087 A US 3435087A US 499974 A US499974 A US 499974A US 3435087D A US3435087D A US 3435087DA US 3435087 A US3435087 A US 3435087A
Authority
US
United States
Prior art keywords
solvent
aromatics
phase
extractor
hydrocarbon
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.)
Expired - Lifetime
Application number
US499974A
Other languages
English (en)
Inventor
Donald B Broughton
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.)
Universal Oil Products Co
Original Assignee
Universal Oil Products 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 Universal Oil Products Co filed Critical Universal Oil Products Co
Application granted granted Critical
Publication of US3435087A publication Critical patent/US3435087A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids

Definitions

  • This invention relates to a process forthe separation of hydrocarbon mixtures With the aid of a selective solvent for the purpose of separating and recovering the aromatic hydrocarbon components of the mixture.
  • the process of the ⁇ present invention serves to segregate the particular species of aromatic hydrocarbons, such as benzene, toluene and/ or C3 aromatics from other classes of hydrocarbons that are normally contained in petroleum distillates, and utilizes a solvent which may be indeiinitely recycled in the system, yields the desired hydrocarbon product in a. state of high purity and separates the same substantially in its entirety from the feed stocks charged to the process.
  • aromatic hydrocarbons such as benzene, toluene and/ or C3 aromatics
  • the present invention is concerned with an improvement in the type of a separation process wherein a feed comprising a mixture of various classes of hydrocarbons having about 75% by weight of aromatic hydrocarbons is introduced Ainto an extraction zone at an intermediate point thereof and is countercurrently contacted therein with a solvent selective for aromatic hydrocarbons, a ratiinate phase comprising substantially all of the non-aromatic hydrocarbons in the feed stock is Iremoved from one end portion of the extraction zone at which the solvent is introduced, a sufficient portion of said ratiinate is recycled to said intermediate point to make the overall mixture of feed and recycled rafl'inate immiscible with the solvent, an extract phase comprising the aromatic components of the feed stocks dissolved in the selective solvent is removed from the other end portion lof the extraction zone and the aromatic solute is subsequently recovered by stripping and fractionating the extract phase.
  • the extract phase is substantially freed, prior to its removal from the extraction zone, of substantially all of the nonaromatic components dissolved by the solvent from the feed stock by introducing a light hydrocarbon which is more volatile in the presence of the solvent than either the 4aromatic or rafiinate components of the feed stock into the extraction zone at a point between the point of removal of extract phase and the point of introduction of the feed stock and displacing into the raiiinate stream the residue of non-aromatic components dissolved in the solvent from the feed stock and replacing in the extract stream the more volatile light hydrocarbon, thereafter separating the more volatile light hydrocarbon contained in the resultant extract phase by stripping the extract after its removal from the extraction zone.
  • this invention relates to a process for the separation and recovery of aromatic hydrocarbons from a hydrocarbon mixture having an aromatics content of at least by weight which comrises: contacting the mixture with a suiiicient amount of rathnate phase from a source hereinafter described to produce an overall mixture which is mmiscible with a lean sulfolane-type solvent; introducing the lean sulfolane solvent into an upper point in the height of an extraction zone; introducing the overall mixture into an intermediate point in the height of the extraction zone and countercurrently contacting said overall mixture therein with the sulfolane solvent at an elevated temperature and at a pressure suiiicient to maintain said solvent and said mixture in substantially liquid phase thereby forming a liquid rainate phase and a liquid extract phase; removing the ratiinate phase from the upper portion of said zone and recycling a sufiicient portion of the rainate phase back to said hydrocarbon mixture to produce said overall mixture; countercurrently contacting the extract phase in the lower
  • Solvent extraction processes for the recovery of aromatic hydrocarbons from hydrocarbon mixtures have been known for many years. This is usually accomplished by processes such as extractive distillation or alternately by countercurrently contacting the feed with a solvent selected for aromatics in the liquid phase within an extractor.
  • the present invention relates to the latter process. If the feed stock non-aromatic components present in the extract phase are not displaced in the extraction Zone, the heavier of these components will not be readily stripped out of the aromatic-solvent mixture in the extractive stripper and due to their similarity of boiling points will dilute the ultimate aromatic purity.
  • the feed is introduced into flow conduit 1 where it flows into an intermediate point in extractor 2.
  • the feed is introduced into the extractor about 1/s of the way along its height from the bottom. This permits the feed to contact the solvent in the upper of the extractor and permits the extract phase to Contact the light hydrocarbon backwash stream in the bottom 1/3 of the extractor.
  • Additional non-aromatic hydrocarbon from a source described hereinafter flows through flow conduit 37 and mixes wtih the feed prior to entering extractor 2. This additional hydrocarbon flows at a sufficiently high rate to make the overall mixture entering the extractor immiscible with the solvent.
  • Lean solvent is introduced into the upper part of extractor 2 through ilow conduit 20 whereupon the lean solvent countercurrently contacts the overall mixture.
  • the extractor is maintained at an elevated temperature and pressure sufficient to maintain the solvent and the feed mixture in the liquid phase. Since the solvent has a selectivity for the aromatics and the solvent is immiscible with the feed and additional hydrocarbon ture, aromatics will preferentially dissolve into the solvent as the solvent passes downflow through the the extractor the aromatics concentration therein gradually increases. Appropriately, the solvent that is iirst introduced into the extractor is called lean solvent and the solvent containing dissolved aromatics is called the fat solvent.
  • the feed and additional hydrocarbon mixture phase passes upflow through the extractor since it is less dense than the solvent phase and the extractor contains suitable means to efciently contact the hydrocarbon phase and the solvent phase.
  • the fat solvent called the extract phase passes into the lower 1/3 of the extractor Where it countercurrently contacts an immiscible light hydrocarbon stream called the backwash.
  • the backwashing step results in the displacement from the extract phase into the backwash hydrocarbon phase of the non-aromatic feed components present in the extract phase. It must be remembered that sulfolanetype solvents will dissolve some non-aromatics along with the aromatics of the feed and the object of the backwasning is to displace the heavier feed non-aromatic hydrocarbons with the lighter hydrocarbons.
  • the backwashing is accomplished by introducing the light hydrocarbon into the lower point of extractor 2 through flow conduit 11.
  • the backwashed extract phase is withdrawn from the lower portion of extractor 2 through ow conduit 3 where it is sent to extractive stripper 4.
  • Stripper 4 is able to remove the non-aromatic components of the extract phase because the presence of the solvent in the stripper has less effect on the boiling point of the nonaromatic compounds dissolved in the solvent than it does on the aromatic compounds also dissolved in the solvent. In general, the solvent tends to retain in solution the more soluble aromatic component, even at temperatures considerably above the normal boiling point of the aromatics alone. However, when processing feed stocks of wider boiling ranges, the stripper will effectively remove the lighter non-aromatics overhead but will have diiculty in removing the heavier non-aromatics overhead without also vaporizing the lighter aromatics.
  • the heavier non-aromatics are displaced by the lighter non-aromatic hydrocarbons in the backwash step to permit the lighter non-aromatics to be readily vaporized in the stripper.
  • Light paraffins are less effective in displacing heavy naphthenes than light naphthenes and accordingly it is preferred that the light backwash material contain an appreciable concentration of naphthene-at least about phase. Thus, upper Z/a of 5%.
  • the ratio of the solvents selectivity for naphthene compared to a paraffin of the same carbon number is about 1.4 to 1.0.
  • the selectivity of saturated sulfolane for said naphthene decreases by a factor of about 1.2 per carbon atom.
  • a light naphthene containing backwash material is eicient and highly satisfactory to displace the heavier non-aromatics from the extract phase.
  • the stripper is operated at elevated temperatures and intermediate pressures (relative to the extractor pressure) in order to remove substantially all of the non-aromatics, some of the water and aromatics and a small amount of the solvent overhead.
  • This overhead stream is removed from stripper 4 through iiow conduit 5 where it passes through condenser 6, ow conduit 7 and into stripper receiver 8.
  • the overhead material is condensed and separated into two phases therein, one a water-solvent phase and the other a light hydrocarbon stream.
  • the light hydrocarbon phase is withdrawn from receiver 8 through ow conduit 11 where it is recycled back to the lower point of extractor 2.
  • the water solvent phase settles in boot 9 where it is withdrawn therefrom through ow conduit 10 and is sent to solvent recovery means not shown.
  • a portion of the bottoms fraction from the stripper flows through ow conduit 38 wherein it passes through reboiler heater 39 and returns to stripper 4.
  • the remaining bottoms portion comprising aromatics and solvent is withdrawn from stripper 4 and passes through How conduit 12, and into solvent recovery column 14.
  • Column 14 is operated at low pressure (relative to the extractor pressure) and elevated temperatures to separate the solvent from the aromatics.
  • the aromatics and a small amount of water are removed as a vapor overhead from column 14 and pass through flow conduit 15, condenser 16 and into column receiver 17.
  • the overhead material is separated into a hydrocarbon phase comprising aromatics and a Water phase.
  • the aromatics are withdrawn from receiver 17 through ow conduit 18 where a portion thereof returns to column 14- as reflux while remaining portion of aromatics is withdrawn through ow conduit 19 as net product.
  • the net product is sent to a series of fractionators to recover the individual aromatics as substantially pure components such as benzene, toluene, ortho-xylene, ethylbenzene, etc.
  • a portion of the bottoms material from column 14 is withdrawn through ow conduit 4t) where it passes through reboiler 41 before returning to column 14.
  • the remaining bottoms portion comprising lean solvent is withdrawn through How conduit 26 wherein a fraction thereof is recycled back to the upper point in extractor 2.
  • the other fraction passes through flow conduit 13 and mixes with the extract phase prior to entering stripper 14. This is done to further improve the separation of aromatics and non-aromatics in the stripper due to extractive distillation since a larger quantity of solvent further increases the difference in boiling point between the non-aromatics and the aromatics in the extract phase.
  • a small but discernible amount of decomposition of solvent and other Sludge forming reactions may occur in the process and it is desirable to remove a small slipstream of lean solvent from ow conduit 2t) through flow conduit 21 and regenerate the solvent in equipment not shown in order to prevent a build-up of sludge.
  • the regeneration preferably is done by rerunning the solvent and thereafter returning the regenerated solvent to oW conduit 20 by means of flow conduit 22.
  • a fraction of this other portion of light raflinate is recycled through ow conduit 31, ow conduit 7 and into ⁇ stripper receiver 8 to supply any make up necessary for loss of light hydrocarbon while the remaining fraction of light raffinate is withdrawn through flow conduit 30 as net product.
  • a heavy raffinate portion is removed from the bottom of splitter 24 through flow conduit 32, flow conduit 33 and reboiler 34 and returns to splitter 24.
  • the net heavy rafnate fraction is withdrawn through ow conduit 35.
  • these naphthenes will be adequate to ehciently displace the heavier non-aromatic components from the extract phase.
  • an outside source of naphthenes preferably of lower boiling point than the components of the .feed stock, rnay be 4initially loaded into the process and splitter 24 is operated to only remove overhead only the lower boiling light naphthenes which are totally recycled to stripper receiver 8.
  • Suitable feed stocks for the process of this invention comprises fluid hydrocarbon mixtures containing at least 75% by weight of aromatics.
  • One source of such feeds is found in the debutanized or depentanized eilluents from reforming reactors.
  • Another source of such feeds is derived from pyrolysis process having light oletins as the principal product.
  • a byproduct liquid is produced from these pyrolysis processes which is rich in aromatics.
  • feed stocks in the carbon number range of from about C5 to about C20 are suitable for use in the process of this invention.
  • the feed stock is in the C6 to C10 range and preferably within the C6 to C8 range.
  • the process of this invention is applicable to many solvents having a selectivity for aromatics such as the glycols, sulfoxides, pyrrolidones, etc.
  • the solvent is a sulfolane-type.
  • the solvent possesses a 5 membered ring, one atom of which is sulfur, the other four being carbon and having two oxygen atoms bonded to the sulfur atom.
  • these solvents may be shown as having the following structural formula:
  • R1, R2, R3 and R4 are independently selected from the group consisting of a hydrogen atom, an alkyl group having up to 10 carbon atoms, an alkoxy radical having up to 8 carbon atoms and an arylalkyl radical having up to 12 carbon atoms.
  • Other solvents preferably included within this process are the sulfolenes such as 2-sulfolene or 3-sulfolene which have the following structure:
  • the sulfolane solvents of this invention may :be made by condensing a conjugated diolefin with sulfur dioxide and then subjecting the resulting product to hydrogenation, alkylation, hydration and/or other substitution or addition reactions.
  • a Z-sulfolene may be made similarly by isomerizing instead of hydrogenating the -product resulting from condensing the conjugated diolen with sulfur dioxide.
  • Suitable solvents which have high selectivity for separating aromatics from non-aromatic hydrocarbons and may be employed in the process of this invention are ZJmethylsulfolane, 2,4-dimethyl-sulfolane, methyl 2- sulfonyl ether, n-aryl-3-sulfonyl amine, z2-sulfonyl acetate, diethylene glycol, various polyethylene glycols, dipropylene glycol, various polypropylene glycols, dimethyl sulfoxide, N -methyl pyrolidone and others.
  • the aromatic selectivity of the sulfolane solvents can be further enhanced by the addition of water to the solvent.
  • the present solvents contain a small amount of water dissolved therein to increase the selectivity of the overall solvent phase for aromatic hydrocarbons over non-aromatic hydrocarbons Without reducing substantially the solubility of the solvent phase for aromatic hydrocarbons.
  • rl ⁇ he presence of water in the solvent composition furthermore provides a relatively Volatile material therein which is distilled from the fat solvent in the extractive stripper to vaporize the last traces of nonaromatic hydrocarbon from the fat solvent stream by steam distillation.
  • the solvent composition preferably contains from about 0.5% to about 20% by weight of a diluent such as Water preferably from about 5% to about depending on the particular sulfolane solvent utilized and the process conditions at which the extractor and extractive stripper are operated.
  • the extractor is operated at elevated temperature and at a suiciently elevated pressure to maintain the feed stock, solvent and light backwash streams in the liquid phase.
  • Suitable temperatures are within the range of from 80 F. to about 400 F. and preferably from about 200 to about 300 F.
  • Suitable pressures are within the range of from about atmospheric pressure up to about 400 p.s.i.g. and preferably from about '50 p.s.i.g. to about 150 p.s.i.g. yIt is preferable that the volume of backwash material introduced into the lower point in the extractor be at least 10% by volume of the extract phase leaving the extractor in order to effectively displace the heavier non-aromatic hydrocarbons from the extract.
  • the extractive stripper is operated at moderate pressures and suciently high reboiler temperatures to drive all the light backwash non-aromatic components and some of the aromatics Water and solvent overhead.
  • Typical stripper pressures are from atmospheric pressure to about 100 p.s.i.g. although generally the top of the stripper is preferably maintained at from about l p.s.i.g. up to about p.s.i.g. 'Ihe reboiler temperature is dependent upon the composition of the feed stock and the solvent.
  • stripper bottom temperatures of from 275 to about 360 F. are satisfactory.
  • the solvent recovery column is operated at low pressures and sufficiently high temperatures to drive the aromatic hydrocarbons overhead and thus producing a lean solvent bottoms stream. Again the choice of operating conditions depends on the feed stock and the solvent composition.
  • the top of the solvent recovery column is operated at vacuum of from about 100 to about 400 lmm. mercury absolute.
  • Low pressures must be ernployed in order to maintain a sufficiently low reboiler temperature to avoid thermal decomposition of the solvent.
  • the reboiler temperature should be maintained below about 360 F. when using saturated sulfolane as the solvent.
  • the apparatus employed in the process of this invention may be any conventional convenient type known to those skilled in the art.
  • the drawing does not show all the pumps, tanks, heat exchangers, valves, bypasses, vents, reboilers, condensers, coolers, control valves, means for actuating control valves and other auxiliaries that may be necessary for the proper operation of the process but the inclusion of which will be evident to those skilled in the art.
  • a hydrotreated ethylene pyrolysis co-product primarily in the C5 lboiling range is employed as the feed stock.
  • the fresh feed is introduced into ow conduit 1 and thereafter into the intermediate point of extractor 2 at a rate of 75.9 moles/hr. consisting of 61.2 moles of vbenzene, 1.4 moles of toluene, and 13.3 moles of non-aromatics.
  • the concentration of aromatics in the fresh feed is about 78% by lweight.
  • About of the non-aromatic fraction consists of naphthenes.
  • Saturated sulfolane containing about 5.2 mole percent water is introduced into the upper point of extractor 2 at a rate of 81.2 moles/ hr.
  • Light backwash containing about 30 mole percent naphthenes is introduced into the lower point of extractor 2 at a rate of 78.4 moles/ hr.
  • the backwash contains about 99 mole percent Cs and the remainder primarily Cfs.
  • a total of 27.4 moles/hr. of raffinate phase is withdrawn from flow conduit 23, of which 13.7 moles/hr. of raffinate passes through iiow conduit 37, pump 36 and returns to iiow conduit 1.
  • the remaining net raffinate phase is withdrawn from extractor 2 through ow conduit 23 at a rate of 13.7 moles/hr.
  • a net bottoms stream is withdrawn from stripper 4 at a rate of 604.6 moles/hr. and sent directly to the solvent recovery column.
  • An overhead hydrocarbon phase is withdrawn from receiver 17 through iiow conduit 19 at a rate of 62.2 moles/hr. and contains 60.9 moles of benzene, and 1.3 moles of toluene.
  • the extractor is a rotary disc contactor and is maintained at a pressure of about p.s.i.g. and a temperature of about F.
  • the stripper is maintained at a top pressure of about 3 p.s.i.g., a top temperature of about 230 F. and a reboiler temperature of about 320 F.
  • the solvent recovery column is maintained at a top pressure of about 375 mm. mercury absolute, a top ternperature of about 120 F. and a 'reboiler temperature of about 320 F.
  • a process for the separation and recovery of aromatic hydrocarbons from a hydrocarbon mixture having an aromatics content of at least 75% by weight r which comprises:
  • R1, R2, R3 and R4 are independently selected from the group consisting of a hydrogen atom, an alkyl group having up to 8 carbon atoms and an arylalkyl radical having up to l2 carbon atoms.
  • the solvent comprises a sulfolene selected from the group consisting of 2-sulfolene and 3-su1folene.
  • the process of claim 3 further characterized in that the light hydrocarbon comprises a iiuid having from about 5 to about 7 carbon atoms per molecule.
  • the improved process of claim 10 further characterized in that the solvent comprises saturated sulfolane and the aromatic concentration in the hydrocarbon feed mixture is at least by weight.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Extraction Or Liquid Replacement (AREA)
US499974A 1965-10-21 1965-10-21 Recovery of aromatics Expired - Lifetime US3435087A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US49997465A 1965-10-21 1965-10-21

Publications (1)

Publication Number Publication Date
US3435087A true US3435087A (en) 1969-03-25

Family

ID=23987535

Family Applications (1)

Application Number Title Priority Date Filing Date
US499974A Expired - Lifetime US3435087A (en) 1965-10-21 1965-10-21 Recovery of aromatics

Country Status (12)

Country Link
US (1) US3435087A (ja)
AT (1) AT273916B (ja)
BE (1) BE688557A (ja)
BR (1) BR6683889D0 (ja)
DE (1) DE1545413C3 (ja)
ES (1) ES332483A1 (ja)
FI (1) FI46733C (ja)
FR (1) FR1500517A (ja)
GB (1) GB1154602A (ja)
NL (1) NL152594B (ja)
SE (1) SE330580B (ja)
YU (1) YU31914B (ja)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4353794A (en) * 1980-11-26 1982-10-12 Uop Inc. Process for the solvent extraction of aromatics and the recovery of an aromatics-free non-aromatic product from a hydrocarbon feedstock
US4543438A (en) * 1984-12-24 1985-09-24 El Paso Products Company Tertiary-butylstyrene recovery
US4543437A (en) * 1984-12-24 1985-09-24 El Paso Products Company Refining of tertiary butylstyrene
US4595491A (en) * 1984-03-14 1986-06-17 Krupp-Koppers Gmbh Process for the separation of aromatic hydrocarbons from a hydrocarbon mixture of varying aromatic content
US4609457A (en) * 1985-02-27 1986-09-02 Uop Inc. Operation of continuous extraction process
US20110306816A1 (en) * 2008-12-09 2011-12-15 Gtc Technology Us, Llc Heavy hydrocarbon removal systems and methods
CN110785390A (zh) * 2017-06-29 2020-02-11 环球油品有限责任公司 用于解吸剂回收的方法和设备

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2034317A1 (en) * 1969-03-14 1970-12-11 Universal Oil Prod Co Solvent extraction of aromatic hydrocracked- - bons
DE102018131061A1 (de) * 2018-12-05 2020-06-10 Endress+Hauser Conducta Gmbh+Co. Kg Verfahren zum Verdünnen einer Probenflüssigkeit und Verdünnungseinheit für eine nachfolgende Analyse

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2407820A (en) * 1943-03-23 1946-09-17 Shell Dev Process for separating aromatic hydrocarbons
US2770663A (en) * 1952-07-30 1956-11-13 Universal Oil Prod Co Solvent extraction of hydrocarbons
US2908726A (en) * 1956-08-06 1959-10-13 Phillips Petroleum Co Solvent extraction with neopentyl glycol

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2407820A (en) * 1943-03-23 1946-09-17 Shell Dev Process for separating aromatic hydrocarbons
US2770663A (en) * 1952-07-30 1956-11-13 Universal Oil Prod Co Solvent extraction of hydrocarbons
US2908726A (en) * 1956-08-06 1959-10-13 Phillips Petroleum Co Solvent extraction with neopentyl glycol

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4353794A (en) * 1980-11-26 1982-10-12 Uop Inc. Process for the solvent extraction of aromatics and the recovery of an aromatics-free non-aromatic product from a hydrocarbon feedstock
US4595491A (en) * 1984-03-14 1986-06-17 Krupp-Koppers Gmbh Process for the separation of aromatic hydrocarbons from a hydrocarbon mixture of varying aromatic content
US4543438A (en) * 1984-12-24 1985-09-24 El Paso Products Company Tertiary-butylstyrene recovery
US4543437A (en) * 1984-12-24 1985-09-24 El Paso Products Company Refining of tertiary butylstyrene
EP0186269A1 (en) * 1984-12-24 1986-07-02 EL PASO PRODUCTS COMPANY (A Delaware Corporation) Refining of tertiary butylstyrene
EP0186270A1 (en) * 1984-12-24 1986-07-02 EL PASO PRODUCTS COMPANY (A Delaware Corporation) Tertiary butylstyrene recovery
US4609457A (en) * 1985-02-27 1986-09-02 Uop Inc. Operation of continuous extraction process
US20110306816A1 (en) * 2008-12-09 2011-12-15 Gtc Technology Us, Llc Heavy hydrocarbon removal systems and methods
US8455709B2 (en) * 2008-12-09 2013-06-04 Gtc Technology Us, Llc Heavy hydrocarbon removal systems and methods
CN110785390A (zh) * 2017-06-29 2020-02-11 环球油品有限责任公司 用于解吸剂回收的方法和设备
EP3645486A4 (en) * 2017-06-29 2021-03-31 Uop Llc METHOD AND DEVICE FOR DESORB RECOVERY

Also Published As

Publication number Publication date
FI46733C (fi) 1973-06-11
BE688557A (ja) 1967-03-31
YU31914B (en) 1974-02-28
DE1545413A1 (de) 1970-01-29
GB1154602A (en) 1969-06-11
ES332483A1 (es) 1967-08-01
FR1500517A (fr) 1967-11-03
AT273916B (de) 1969-08-25
NL152594B (nl) 1977-03-15
YU197366A (en) 1973-08-31
DE1545413C3 (de) 1974-12-19
SE330580B (ja) 1970-11-23
BR6683889D0 (pt) 1973-08-28
FI46733B (ja) 1973-02-28
NL6614901A (ja) 1967-04-24
DE1545413B2 (de) 1974-05-16

Similar Documents

Publication Publication Date Title
US3723256A (en) Aromatic hydrocarbon recovery by extractive distillation, extraction and plural distillations
US4053369A (en) Extractive distillation
US4058454A (en) Aromatic hydrocarbon separation via solvent extraction
US3361664A (en) Flashing and extractively distilling an extract
US3114783A (en) Separation of aromatics from hydrocarbon streams
US4048062A (en) Aromatic extraction with solvent recovery and regeneration
US4401517A (en) Vapor-liquid extractive distillation with dialkyl sulfone/water combination
US3435087A (en) Recovery of aromatics
US3642614A (en) Reduction of soluble contaminants in lean solvent
US2831905A (en) Gamma-butyrolactone as a selective solvent for hydrocarbons
US3844902A (en) Combination of extractive distillation and liquid extraction process for separation of a hydrocarbon feed mixture
US5336840A (en) Process for the separation of aromatic hydrocarbons with energy redistribution
US5073669A (en) Method for aromatic hydrocarbon recovery
US3590092A (en) Method for aromatic hydrocarbon recovery
US3763037A (en) Aromatic hydrocarbon
US4083772A (en) Aromatic hydrocarbon separation process
US3702295A (en) Aromatic hydrocarbon recovery method
US3249532A (en) Solvent extraction of aromatics
US3396101A (en) Solvent extraction of highly aromatic charge stocks
US5022981A (en) Aromatic extraction process using mixed polyalkylene glycol/glycol ether solvents
US2786085A (en) Solvent extraction process applied to feed stocks of high boiling points
US3864244A (en) Solvent extraction with internal preparation of stripping steam
US3422163A (en) Recovery of aromatics from multiple hydrocarbon streams
US4046676A (en) Aromatic hydrocarbon separation via solvent extraction
CA1053601A (en) Extractive distillation