US3627671A - Combination reforming process - Google Patents

Combination reforming process Download PDF

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US3627671A
US3627671A US865011A US3627671DA US3627671A US 3627671 A US3627671 A US 3627671A US 865011 A US865011 A US 865011A US 3627671D A US3627671D A US 3627671DA US 3627671 A US3627671 A US 3627671A
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zone
weight percent
platinum
reforming
catalyst
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Robert H Kozlowski
Robert P Sieg
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ROBERT H KOZLOWSKI
ROBERT P SIEG
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ROBERT P SIEG
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
    • C10G2400/08—Jet fuel

Definitions

  • the present invention relates to a reforming process operated at low pressure. More particularly, the present invention is concerned with a combined low-pressure reforming process and solvent extraction process for producing high yields of gasoline and jet fuel materials.
  • Patent 3,044,950 it is disclosed that increased gasoline yield can be obtained by distilling a hydro-- genated catalytic cracking feedstock into at least two streams, a higher boiling stream and a lower boiling stream, solvent extracting the higher-boiling stream to obtain an aromatic portion and a nonaromatic portion, combining the nonaromatic portion with the lower boiling stream from the distillation zone and catalytically reforming the blend, then combining the effluent from the catalytic reformer with the? aromatic fraction from the solvent extraction zone. Also, in LLS Patent 2,914,457 the solvent extraction of the!
  • the aromatic extract can be used for gasoline and the paraffinic raffinate used as a diesel or jet fuel component.
  • the paraffinic portion can be recycled to the reformer.
  • the feed used to produce high yields of gasoline and jet fuel products by means of the present invention should boil within the range from 150 to 550 F, preferably between 150 to 450 F.
  • the feed may be a straight-run naphtha, a thermally cracked naphtha, a catalytically cracked naphtha, a hydrocrackate, or blends thereof.
  • Hydrogenating the feedstock in a presaturation zone is generally accomplished by contacting the feed with a hydrogenation catalyst which is resistant to sulfur poisoning.
  • a suitable catalyst for the hydrofining process, or hydrodesulfurization process, as it is sometimes referred to. is, for example, an alumina-containing support having associated therewith a minor proportion of molybdenum oxide and cobalt oxide.
  • Other suitable hydrofining catalysts include nickel-molybdenum or nickel-cobalt-molybdenum supported on an alumina carrier or a zeolite carrier or combinations thereof. The catalyst can be pretreated with hydrogen sulfide prior to contact with the feed.
  • Hydrofining or hydrodesulfun'zation is generally conducted at a temperature within the range 700 to 850 F, a pressure of from 200 to 2000 psig, and a liquid hourly space velocity of from 1 to 5.
  • the hydrofining is accomplished in the presence of hydrogen.
  • the hydrogen-to-feed ratio will be from 1000 to 5000 SCF of hydrogen per barrel of feed.
  • the reaction conditions are generally severe enough to convert substantially all the organic sulfur to hydrogen sulfide.
  • the reaction conditions should be severe enough so that the effluent from the hydrofining zone contains less than about 10 ppm organic sulfur, preferably less than about 5 ppm organic sulfur, and more preferably less than about 1 ppm organic sulfur. Any produced H 8 is removed from the feed, preferably prior to fractionation of the feed into the lower-boiling range stream and the higherboiling range stream.
  • the feed preferably containing low amounts of sulfur and other poisons, is fractionated by conventional means known in the art into at least two streams, a first stream boiling within the range of from 150 F to 340 ⁇ ; and a second stream boiling within the range of from 300F to 550F.
  • the first stream could have a boiling range of 150 to 320 F
  • the second stream a boiling range of 320 to 450 F.
  • any H 8, water, or light hydrocarbon gases may be removed as a separate stream.
  • the lower-boiling range stream that is, the stream boiling from within the range of from 150 to 340F is separately processed from the higher-boiling range stream.
  • the first stream is contacted in a reforming zone in the presence of hydrogen at reforming conditions to produce high-octane gasoline.
  • the reforming conditions include a temperature of from 600 to 1100F, preferably from 750 to 1050 F.
  • the pressures will be less than about 300 psig, and preferably less than about 200 psig. Generally the pressure will be above atmospheric, for example, at least 25 psig.
  • Cit-hydrocarbons is decreased. A decrease in the production of light gases represents an increase in the pfoductiqniof significantly more valuable gasoline and/or jet fuel' components.
  • the temperature and pressure in the reforming zone can be correlated with the liquid hourly space velocity (LHSV) to favor any particularly desirable reforming reactions, as, for example, dehydrocyclization or isomerization or dehydrogenation.
  • LHSV liquid hourly space velocity
  • the liquid hourly space velocity will be from 0.1 to 10, and preferably from 1 to 5.
  • a 'Ll'ierefggming process is conducted in the presence of separated from the reformate and recycled to the reaction 1 zone.
  • extraneous hydrogen need not necessarily be added to the reforming process.
  • traneous hydrogen may be used at some stage of the operation, as, for example, during startup. Regardless of the source of the hydrogen, the hydrogen can be introduced into the feed prior to contact with the catalyst or can be contacted simultaneously with the introduction of feed to the reaction zone.
  • the hydrogen need not necessarily be pure hydrogen, but may contain light hydrocarbon gases in admixture therewith. Generally, when hydrogen is recirculated to the reaction zone. some light hydrocarbon gases will be recirculated with the hydrogen. While it is preferred that relatively pure hydrogen be used, difficulty and expense in purifying recycle hydrogen often prevents this from being the case. Hydrogen is preferably introduced into the reforming reactor at a rate which varies from 0.5 to moles of hydrogen per mole of feed,
  • the reforming conditions vary depending on the feed used, whether highly aromatic, paraffinic or naphthenic, and upon the desired octane rating of the product. Generally it is preferred that the reforming process be operated at high severity conditions, that is, conditions which will result in the production of a gasoline product having at least 90 Fl clear octane rating, and more preferably at least 95 F-l clear octane rating.
  • the reforming zone may consist of one reactor or several reactors containing a hydrogenation-dehydrogenation catalyst.
  • the reforming zone will comprise several reactors, preferably at least three reactors, in series.
  • the hydrocarbon feed is preheated and mixed with hydrogen and then passed through the plurality of reaction zones containing catalyst. Generally in all but the last stages the reactions are endothermic; hence the hydrocarbon feed passing between the reactors is reheated to the desired conversion temperature. Reformed hydrocarbons are recovered from the terminal reactor and hydrogen is separated therefrom and a portion thereof recycled to the reactorts).
  • the catalyst which finds use in reforming comprises a platinum group component associated with a porous solid carrier.
  • the catalyst comprises a platinum group component, e.g., platinum, palladium, iridium, ruthenium, etc., supported with a porous inorganic oxide as, for example, alumina.
  • the platinum group component will be present in an amount of from 0.01 to 3 weight percent and preferably 0.01 to 1 weight percent.
  • the weight percent of the platinum group component is calculated as the metal regardless of the form in which it exists on the catalyst.
  • the platinum group component embraces all the members of Group VIII of the Periodic Table having an atomic weight greater than 100 as well as compounds and mixtures of any of these. Platinum is the preferred component because of its better reforming activity,
  • Porous sdHiTam'ers wi'izrshaaaaana us f ofieform ing are generally the inorganic oxides, particularly inorganic oxides having surface areas of 50 to 750 m lgm, preferably.
  • the carrier can be a natural or a synthetically produced inorganic oxide or combination of inorganic oxides.
  • Typical acidic inorganic oxide supports which can be used are the naturally occurring aluminum silicates, particularly when acid treated to increase the activity, and the synthetically-produced cracking supports, such as silicaalumina, silica-zirconia, silica-alumina-zirconia, silicamagnesia, silica-alumina-magnesia, and crystalline zeolitic aluminosilicates.
  • the catalysts have low cracking activity, that is, have limited acidity.
  • alumina be present. Any of the forms of alumina suitable as a support for reforming catalysts can be used, e.g., gamma-alumina, eta-alumina, etc.
  • alumina can be prepared by a variety of methods for purposes of this invention.
  • the alumina can be prepared by adding a suitable alkaline agent such as ammonium hydroxide to a salt of aluminum, such as aluminum chloride, aluminum nitrate, etc, in an amount to form aluminum hydroxide which on drying and calcining is converted to alumina.
  • Alumina may also be prepared by the reaction of sodium aluminate with a suitable reagent to cause precipitation thereof with the resulting formation of aluminum hydroxide gel. Also, alumina may be prepared by the reaction of metallic aluminum with hydrochloric acid, acetic acid. etc.. in order to form a hydrosol which can be gelled with a suitable precipitating agent, such as ammonium hydroxide. followed by drying and calcination.
  • a suitable precipitating agent such as ammonium hydroxide.
  • rhenium be present, for example, in an amount of from 0.01 to 5 weight percent and more preferably 0.01 to 2 weight percent. Regardless of the form in which rhenium exists on the catalyst, whether as metal or compound, the weight percent is calculated as the metal. Rhenium significantly improves the yield stability of the platinum-containing catalyst; that is, a process using a platinum-rhenium catalyst has a significantly lower yield decline throughout the reforming process than a catalyst comprising platinum without rhenium.
  • the platinum-rhenium catalyst is more fully described in U.S. Patent 3,415,737, which is incorporated herein by reference thereto.
  • the catalyst comprising the platinum group component can be prepared by a variety of methods; that is, the platinum group component can be associated with the porous solid carrier by impregnation, ion-exchange, coprecipitation, etc. Generally it is preferred to incorporate the platinum group component by impregnation.
  • the rhenium component can also be associated with the carrier by various techniques, e.g., impregnation, ion-exchange, coprecipitation, etc.
  • the platinum group component and rhenium component are associated with the carrier by impregnation, either simultaneously or sequentially.
  • platinum group compounds for use in impregnation include chloroplatinic acid, ammonium chloroplatinates, polyammineplatinum slats, palladium chloride, etc.
  • Suitable rhenium components are perrhenic acid, ammonium or potassium perrhenates, etc. W W
  • the catalyst used in reforming can be promoted by the addition of halides, particularly fluoride or chloride. Bromides may also be used.
  • the halides provide a limited amount of acidity to the catalyst which is beneficial to most reforming operations.
  • a catalyst promoted with halide preferably contains from 0.1 to 3 weight percent total halide content.
  • Halides can be incorporated onto the catalyst carrier at any suitable stage of catalyst manufacture, e.g., prior to or following incorporation of the platinum group component and/or the rhenium component. Halide can also be incorporated onto the catalyst during incorporation of the platinum group component or rhenium component.
  • the second stream from the fractionation zone that is, the feed stream boiling with the range of from 300 to 550 F, is passed to a solvent extraction zone in contact with a selective solvent for aromatic hydrocarbons which is relatively immiscible with nonarornatic hydrocarbons.
  • the solvent should have relatively selective solubility for the aromatics at the elevated temperature of the extraction, preferably in excess of 200 F, and a low solubility at the temperature of operation of the desorbing procedure, generally in the neighborhood of F, wherein aromatics are separated from the solvent.
  • a preferred solvent is diethylene glycol, which may be used alone or diluted with, say, 2 to 10% by weight of water.
  • Representative of others of the glycol solvents which may be utilized with somewhat less advantageous results are ethylene glycol. triethylene glycol, tetraethylene glycol and dipropylene glycol.
  • the particularly preferred solvents are the sulfolanes.
  • sulfolane itself and many of its derivatives, such as hydrocarbon-substituted sulfolanes, including alkyl sulfolanes, e.g., 3-methylsulfolane, preferably containing not more than 14 carbon atoms; hydroxy sulfolanes such as 3-sulfolanol, 3-methyl-4-sulfolanol, etc.; sulfolanyl ethers such as methyl-3-sulfolanyl ether; and sulfolanyl esters such as 3-sulfolanyl acetate.
  • alkyl sulfolanes e.g., 3-methylsulfolane, preferably containing not more than 14 carbon atoms
  • hydroxy sulfolanes such as 3-sulfolanol, 3-methyl-4-sulfolanol, etc.
  • sulfolanyl ethers such as methyl-3-sulf
  • the extraction zone there is formed an extract phase enriched in aromatics and a raffinate phase containing predominantly nonaromatic hydrocarbons.
  • the extract phase or fraction upon its removal from the extraction zone is cooled to effect the formation of a solvent phase and a hydrocarbon phase.
  • Other means can be used to extract the solvent phase and the aromatic phase as, for example, distillation. However, generally sufficient separation can be accomplished by cooling the extract mixture of aromatic and solvent.
  • the aromatic phase may be water washed to remove final amounts of solvent.
  • the raffinate fraction from the solvent extraction zone is also generally water washed to remove any solvent dissolved therein, dried, and at least a portion thereof then used as a jet fuel component.
  • the raffinate fraction will be enriched in nonaromatic components, that is. enriched in substantial amounts of paraffins, which make valuable jet fuel components.
  • At least a portion of the extract or aromatic fraction from the solvent extraction zone is blended with the product from the reforming zone to produce a high-octane gasoline product.
  • the feed to be extracted can be fed to a rotating disc contactor containing sulfolane. 1n the rotating disc contactor, both extraction of aromatics by the sulfolane and separation of the extract fraction and the raffinate fraction occur.
  • the raffinate fraction is removed from the contactor and can then be further treated in another rotating disc contactor containing sulfolane to remove any remaining aromatics. Generally, this is not necessary for purposes of this invention.
  • the raffinate fraction is generally passed from the rotating disc contactor to a water wash column to remove any sulfolane. At least a portion of the raffinate recovered from the water wash column can then be used as a jet fuel component.
  • the extract fraction enriched in aromatics is recovered from the rotating disc contactor and then passed to a distillation column to remove sulfolane from the aromatics. At least a portion of the aromatics fraction may then be admixed with the gasoline fraction from the low pressure reformer. Sulfolane will generally be purified and recycled to the rotating disc contactor. It is not necessary for purposes of the present invention to use severe solvent extraction conditions, i.e., conditions to result in complete separation of aromatics from nonaromatics.
  • a catalyst comprising a platinum group component in association with a porous solid carrier at reforming conditions, including a pressure greater than about 300 psig, preferably greater than about 350 psig.
  • the catalyst can be similar to the catalyst used in the low pressure reforming zone and and will preferably be a platinum-rhenium-alumina catalyst.
  • the other reforming conditions are correlated with the pressure to produce a high-octane gasoline having at least 90 F 1 clear octane rating.
  • the raffinate fraction from the solvent extraction zone may be passed to a distillation column for separation into two fractions, ajet fraction boiling within the range from about 300F to about 450 F and a lighter fraction boiling below about 300 F, said jet fraction being used as a jet fuel component and said lighter fraction being blended with the gasoline product from the low-pressure reforming zone.
  • the aromatics extract from the solvent extraction zone is still blended with the gasoline product from the low-pressure reforming zone.
  • a hydrocarbon feedstock boiling within the range from 150 to 550 F is passed by line 1 into hydrofining zone 2.
  • the hydrofining zone will contain a catalyst, for example cobalt oxide and molybdenum oxide supported on alumina, and the reaction conditions will be such as to substantially convert any organic sulfur to H S.
  • the hydrofining operation is conducted in the presence of hydrogen provided by means of line 3, and the hydrogen may come from the low-pressure reforming zone 4 or from any other hydrogen source.
  • the effluent from the hydrofining zone may be purified in a separation zone or distillation zone (not shown in the Figure).
  • the hydrocarbon feed is then passed by line 5 to a fractionation zone 6 wherein it is separated into at least two streams, a first stream boiling within the range of from 150F to 340F and a second stream boiling within the range of from 300 to 550 F.
  • the first stream is passed by line 7 to reforming zone 4 in contact with a platinum-group component catalyst at reforming conditions including a pressure of less than about 300 psig.
  • Hydrogen is made available to the reforming zone by means of line 8.
  • the hydrogen may be bottled hydrogen or hydrogen separated from the effluent from the reforming zone, etc.
  • the second stream is passed by line 9 into solvent extraction zone 10 in contact with a solvent selective for aromatics, preferably sulfolane.
  • the aromatic extract is removed from the solvent extraction zone by line 11 and is freed of solvent by conventional means (not shown in the Figure) and at least a portion passed into admixture with the effluent in line 12 from reforming zone 4.
  • the blend is passed by line 13 to gasoline storage.
  • the raffinate fraction from the solvent extraction zone is recovered by line 14 and, after suitable treatment to remove any solvent dissolved therein (not shown in the Figure) is used as a component forjet fuel.
  • a feed boiling from 173 to 426F and containing 39 volume percent paraffins, 43.6 volume percent naphthenes and 17.4 volume percent aromatics, having an F-l clear octane rating of 52.5 and being essentially free of sulfur (less than 0.1 ppm) is reformed in the presence of a catalyst comprising platinum and rhenium in association with alumina.
  • the platinum-rhenium-alumina catalyst comprises 0.3 weight percent platinum, 0.3 weight percent rhenium and 0.6 weight percent chloride, the remainder being alumina.
  • the reforming process conditions include a feed rate, in barrels per day (BPD), of about 20,000, a liquid hourly space velocity of 1.5, a hydrogen to hydrocarbon mole ratio of 6, and a pressure of 500 psig. The reforming is run to produce a gasoline product having a F-l clear octane rating.
  • a feed substantially as described above, is fractionated in a distillation column into two fractions, a lower boiling range fraction and a higher boiling range fraction.
  • the lower boiling range fraction boils from about 173 to 329F and contains 42.2 volume percent paraffins, 42.6 volume percent naphthenes. and 15.2 volume percent aromatics.
  • the F-l clear octane rating is about 55.
  • the lowerboiling fraction is then reformed in the presence of a platinum-rhenium-alumina catalyst containing 0.3 weight percent platinum, 0.3 weight percent rhenium, and 0.6 weight percent chloride, the remaining portion being alumina.
  • the reforming conditions include a feed rate to the reformer of about 15,000 barrels per day (BPD), a liquid hourly space velocity of 2, a hydrogen to hydrocarbon mole ratio of 6, and a pressure of 200 psig. A product of about 100 F--] clear octane rating is produced.
  • the higher-boiling fraction from the distillation column boils within the range of from about 329 to 426 F. and is passed to a sulfolane extraction unit at a rate of about 5000 BPD.
  • the extraction zone is a rotating disc contactor and is operated at a temperature of about 240 F.
  • the solvent/ oil weight ratio is about 2.711.
  • the amount of aromatics extract, after removal of sulfolane and drying, is about 1470 BPD of 77.6 volume percent aromatics content.
  • This aromatics extract is combined with the gasoline product from the low pressure reformer.
  • the amount of raffinate fraction from a sulfolane extraction zone, after treatment to remove any sulfolane is about 3530 BPD of 2L3 volume percent aromatics content.
  • the raffinate fraction is of good jet fuel quality having a 25 mm smoke point.
  • the results of the combination of the low pressure reforming-solvent extraction process is tabulated under column B in the Table.
  • a process for increasing the yield of valuable gasoline and jet fuel products from a feed boiling within the range from F. to 550 F. which comprises:

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4894144A (en) * 1988-11-23 1990-01-16 Conoco Inc. Preparation of lower sulfur and higher sulfur cokes
FR2635112A1 (fr) * 1988-08-02 1990-02-09 Inst Francais Du Petrole Procede de fractionnement et d'extraction d'hydrocarbures permettant l'obtention d'une essence a indice d'octane ameliore et d'un kerosene a point de fumee ameliore

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2848377A (en) * 1953-10-19 1958-08-19 Standard Oil Co Platinum catalyst composite employed in the hydroforming of a naphtha
US3201340A (en) * 1962-01-23 1965-08-17 Sinclair Research Inc Method and apparatus for the catalytic reforming of naphthas in series
US3392107A (en) * 1966-01-05 1968-07-09 Sinclair Research Inc Process for reforming naphthene and paraffin containing hydrocarbons in the naphtha boiling point range in several stages to obtain a high octane gasoline
US3424669A (en) * 1967-01-03 1969-01-28 Exxon Research Engineering Co Reforming-aromatization process with sulfided catalyst
US3507781A (en) * 1969-04-24 1970-04-21 Chevron Res Startup procedure for a platinumiridium reforming process

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2848377A (en) * 1953-10-19 1958-08-19 Standard Oil Co Platinum catalyst composite employed in the hydroforming of a naphtha
US3201340A (en) * 1962-01-23 1965-08-17 Sinclair Research Inc Method and apparatus for the catalytic reforming of naphthas in series
US3392107A (en) * 1966-01-05 1968-07-09 Sinclair Research Inc Process for reforming naphthene and paraffin containing hydrocarbons in the naphtha boiling point range in several stages to obtain a high octane gasoline
US3424669A (en) * 1967-01-03 1969-01-28 Exxon Research Engineering Co Reforming-aromatization process with sulfided catalyst
US3507781A (en) * 1969-04-24 1970-04-21 Chevron Res Startup procedure for a platinumiridium reforming process

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2635112A1 (fr) * 1988-08-02 1990-02-09 Inst Francais Du Petrole Procede de fractionnement et d'extraction d'hydrocarbures permettant l'obtention d'une essence a indice d'octane ameliore et d'un kerosene a point de fumee ameliore
EP0354826A1 (fr) * 1988-08-02 1990-02-14 Institut Français du Pétrole Procédé de fractionnement et d'extraction d'hydrocarbures permettant l'obtention d'une essence à indice d'octane amélioré et d'un kérosène à point de fumée amélioré
US4894144A (en) * 1988-11-23 1990-01-16 Conoco Inc. Preparation of lower sulfur and higher sulfur cokes

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