US2905619A - Upgrading gasoline - Google Patents

Upgrading gasoline Download PDF

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Publication number
US2905619A
US2905619A US594592A US59459256A US2905619A US 2905619 A US2905619 A US 2905619A US 594592 A US594592 A US 594592A US 59459256 A US59459256 A US 59459256A US 2905619 A US2905619 A US 2905619A
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fraction
gasoline
zone
isomerization
line
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US594592A
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English (en)
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Robert E Sutherland
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Universal Oil Products Co
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Universal Oil Products Co
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Priority to US594592A priority Critical patent/US2905619A/en
Priority to GB19947/57A priority patent/GB809635A/en
Priority to DEU4615A priority patent/DE1057711B/de
Priority to ES0236274A priority patent/ES236274A1/es
Priority to BE558772A priority patent/BE558772A/fr
Priority to FR1178064D priority patent/FR1178064A/fr
Application granted granted Critical
Publication of US2905619A publication Critical patent/US2905619A/en
Priority to MY57/62A priority patent/MY6200057A/xx
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    • 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
    • C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
    • C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only
    • 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

Definitions

  • This invention relates to a novel process for upgrading 'gasoline and more particularly to an integrated process in which a gasoline is separated into selected fractions and the selected fractions are subjected to independent and selected conditions to produce a final product of high octane value.
  • the automobile industry is manufacturing engines of greater horsepower and accordingly higher compression ratios. These engines require gasolines of higher octane value in order to operate satisfactorily therein. This, in turn, challenges the petroleum industry to produce gasolines of even higher octane values than the high octane gasolines presently being produced.
  • the present invention provides a novel combination process of mutually related and interdependent steps whereby gasoline is upgraded to these higher octane values.
  • a gasoline is fractionated to separate a C6 and lighter fraction and a C7 and heavier fraction.
  • the C7 and heavier fraction is subjected to catalytic reforming to upgrade this fraction of the gasoline.
  • the reformed products are fractionated to separate a C6 and lighter fraction, which fraction is combined with the previously separated C6 and lighter fraction, and the mixture is subjected to isomerization to convert the low octane normal paraiiins into high octane branched parafns.
  • the isomerized products are combined with the reformed products to form a final product of high octane value.
  • Catalytic reforming of gasoline serves to considerably improve its octane value.
  • the pentanes contained in the gasoline fraction undergo only minor conversion when subjected to reforming in admixture with the higher boiling gasoline components. Therefore, it
  • the pentanes and hexanes are fractionated to separate thevhigh octane paraiiins from the low octane parains, and the latter are isomerized into high octane branched chain parains.
  • the high octane paraftns then are blended with the reformed gasoline fraction to produce a final blend of high octane value.
  • isopentane has a Research octane value, when leaded with 3 cc. of tetraethyl lead, of 103.5.
  • normal pentane has a leaded octane number of only 85. It is readily seen that the presence of the low octane normal pentane in the final gasoline blend reduces the overall octane num- Similarly, normal hexane has a leaded octane number of only 65.3, whereas the branched chain hexanes have leaded octane numbers in excess of 93.
  • these low octane components are converted into high octane products and, when blended in the final gasoline, serve to produce a final gasoline of considerably higher octane number thanpreviously attained.
  • the present invention provides an integrated combination yof isomerization and catalytic reforming for the production of high octane gasoline.
  • the high octane product cannot be achieved by catalytic reforming alone, except by using extremely severe operating conditions which, in turn, results in excessive losses in yield, as well as in low catalyst life. These excessive losses and low catalyst life prohibit any practical or commercial utilization ofthe catalytic reforming process in this manner for obvious economic reasons.
  • the novel process of the present invention selectively separates the low octane components and independently converts them into high octane components.
  • improved results include higher overall yields of high octane gasoline.
  • operation of the catalytic reforming at less severe conditions than otherwise would be required, with the concomitant high yields and long catalyst life in the reforming step of the process, the greater exibility in ⁇ operation to permit the processing of a variety of Igasoline charge stocks, as well as producing gasolines of even higher octane numbers as may be required to meet market demands of the future.
  • the novel method of the present invention the low octane components are converted in the absence of the high octane components, and therefore any possible undesired conversion of the high octane components is avoided.
  • the gasoline charge is introduced to the process through line 1 and is directed into dehexanizer 2.
  • the gasoline charge has a boiling range of from C5 to about 400 F., although the end point may be higher, ranging up to about 450 F.
  • the gasoline charge preferably is a saturated gasoline and thus may comprise straight run gasoline, natural gasoline, etc., or hydrogenated unsaturated gasolines, such as cracked gasoline, Coker distillate, etc., which previously had been subjected to desulfurization-hydrogenation, or a mixture of these gasolines.
  • reforming zone 4 is illustrated as a single zone, it is understood that this system will comprise heaters, heat exchangers, a series of reaction zones, generally 3 or 4, coolers and receivers.
  • the reforming is effected at a temperature of from about 800 to about 1050 F., at a pressure of from about to about 1000 pounds or more per square inch, a liquid hourly space velocity of from about 0.5 to 10, and in the presence of hydrogen in a mol ratio to hydrocarbon of from about 0.5 to 20.
  • a v ⁇ particularly preferred catalyst comprises ⁇ a composite of alumina, platinum in a concentration of from about 0.2 to about 1% by Weight and combined halogen in a concentration of from about 0.2 to about 1% by vweightof the nal catalyst.
  • the halogen preferably 'comprises urine and/or chlorine.
  • the reforn'edprducts are withdrawn from zone 4 through line 5 and are directed to receiver 6.
  • hydrogencontaining gas is withdrawn through nd while all or a portion may be removed from the process through valve 7, at least a portion of the hydrogen is recycled by way of line 8, valve 8', and line 3 Within the 4system for further use therein.
  • the C5 an'dCs hydrocarbons separated in zone 2 are withdrawn therefrom through line 17 and are commingled with the C5 and C6 hydrocarbonswithdrawn fromzone 13 and directed through line 14, the mixture then being directed by way vof line 18 and valve 19 to splitter Z0.
  • Splitter 20 functions to separate an overhead fraction comprising pentanes and a lower fraction comprising hexanes.
  • the pentanes Yseparated in zone 20 are withdrawn therefrom through line 21 and are directed through line v2.2 toideisopentanizer Z3.
  • the deisopentanizer functions to split an overheadv fraction comprising isopentane from a bottoms fraction comprising normal pentane.
  • zone 23Y functions to separate the isopentane originally containedin the gasoline charge, as well as the isopentane contained in'thereformed products;
  • the isopentane separated in zone 23 is vwithdrawn therefrom through line 24 and, in a preferred embodiment :of the invention, ⁇ at least av portion'thereof isdirected to gasoline blending zone 16.
  • 'Isopentane has a leaded Research 'octane number of sfr'abl Component foi' the inal ⁇ gasoline blend.
  • Isomerization zone 27 likewise comprises suitable heater, heat exchanger, reactor, cooler, etc. In a preferred embodiment of the invention, only one reactor will be required because the overall heat of reaction is low. Any suitable isomerizatin catalyst may be utilized in zone 27.
  • AY-preferred catalyst comprises a platinumcontaining composite "and still 4more Yparticularly the alumina-platinurnLcombined halogen 'catalyst described 4above Vfor vuse vin the reforming zone. With thesejcatalysts, isomerization ⁇ of pentane generally fis effected at a temperaturejof from aboutf700 toabgutgSOF.
  • the consumption or p ⁇ rodc tion of hydrogen is of very low order andthe hydrogen preferably is recycledwithin theisonierization by well-known means, not illustrated, or it mayfbe supplied, either continuously or intermittently,A from the reforming system.
  • the isomerzed pentane fraction iswithdrawnjrom zone 27 through line 28 and itis returnedbyway of line 22 to deisopentanizer 2 3.
  • the deisopentanizer serves to separate the isopentaneformed in zone 2 7, as well as the isopentane'contained in the originalgasoline charge and that produced in the reforming reaction.
  • the isopentane is directed through line 24 into gasoline blendingzone 16 pentane is withdrawn from the lower portion of zon e 23 recycled in zone 27 for isomerizaaluminum chloride, aluminum bromidetzino chloride,
  • the metal halide catalysts are cornposited with a suitable carrier such asjalurnina, bauxite, clay, etc., and utilized as a fixed bedofcatalyst in the reaction zone.
  • a suitable carrier such asjalurnina, bauxite, clay, etc.
  • a these catalysts may be utilized in liquid form,
  • the isomerization reaction generallyis effected at a temperature of from about to abo ut 300 F. It is understood that the various isomerization catalysts are not necessarily equivalent and that the preferred catalyst comprises the platinum-containing catalyst hereinbefore described.
  • the hexanes separated in'splitter 20 are withdrawn rherefram'through line 7.9 and are airectedt aeisfoheiranizer.
  • the deisohexanizer serves to separate the lower boiling higher octane branched chain hexanes originally present in the gasoline charge to the process, as well as that produced in the reforming step of the process.
  • the normal hexane and higher boiling C6 components are withdrawn from zone 30 through line 32. and are directed through valve 33 to isomerization zone 34.
  • zone 34 the hexanes are subjected to isomerization under optimum conditions which are independently controlled to obtain maximum conversion.
  • This isomerization zone will be similar to that hereinbefore described in connection with the pentane isomerization, and may utilize the same type of catalyst hereinbefore described.
  • the catalyst comprises the platinum-containing composite hereinbefore described.
  • the conditions in this zone while being within the range hereinbefore described, will be selected to effect maximum conversion to the desired products.
  • the isomerization products from zone 34 are withdrawn from line 35 and are directed through valve 36 to gasoline blending zone 16.
  • the isomerized product from zone 34 will contain cyclic compounds including methyl cyclopentane, cyclohexane, benzene, etc., in small but varying concentrations. These cyclic compounds are of high octane value and, in the preferred embodiment of the invention, are included in the final gasoline product of the process.
  • the nal gasoline blend comprises reformed gasoline, isopentane, low boiling high octane branched chain hexanes and isomerized hexanes.
  • the gasoline blend is of low vapor pressure and therefore will permit the introduction of butanes and additional isopentanes to raise the vapor pressure to the desired pounds R.V.P. or thereabouts. The introduction of these materials further increases the octane rating of the final gasoline product.
  • the final gasoline blend will have a leaded Research octane number of above 95 and may range up to 102 or even higher.
  • hexanes In conventional fractionation, a small amount of hexanes will be carried over in the overhead fraction from splitter and will accumulate in the bottoms fraction in deisopentanizer 23. In order to avoid the buildup of the hexanes in this step of the process, a drag stream of the bottoms fraction is continuously or intermittently directed through line 27 and valve 38 to be returned by way of lines 39 and 19 to splitter 20. In this manner, the hexanes will be removed from the C5 fraction and will not build up in the pentane isomerization system.
  • the splitter serves to separate pentanes from hexanes and the former is directed to deisopentanizer 23, while the latter is directed to deisohexanizer 30.
  • the bottoms fraction from -both of these fractionators are returned to the isomerization zone. This is accomplished by passing the bottoms from zone 23 through line 25, line 44, valve 45 and line 32 to zone 34, and passing the bottoms fraction from zone 30 through line 32 and valve 33 to zone 34.
  • the use of a single isomerization zone for converting both the pentanes and hexanes generally is not as desirable as employing separate zones for these isomerizations.
  • the octane value of the nal gasoline will be suicient to meet prevailing market requirements and therefore the use of a single isomerization zone may be satisfactory.
  • the pentane-hexane fraction being directed through line 18 is passed through valve 19 into zone 2t), and subjected to separation therein as well as in deisopentanizer 23 and deisohexanizer 30.
  • the normal pentane is directed through lines 25, 44 and 32 to isomerization zone 34, instead of being subjected to separate isomerization as in the particularly preferred embodiment of the invention.
  • the effluent isomerization products from 'zone 34 are directed through lines 35, 42 and 46, valve 47 and line 29 and deisohexanizer 30 for separation of the low boiling high octane branched chain hexanes from normal hexane, the latter to be recycled by way of line 32 to zone 34 for further isomerization.
  • deisohexanizer 30 When utilizing recycle type operation of the isomerized hexanes, there may be a buildup of heptanes in deisohexanizer 30. This is similar to the possible buildup of hexanes in deisopentanizer 23 heretofore described.
  • a drag stream is directed by way of line 48, valve 49 and line 1 to dehexanizer 2.
  • dehexanizer 2 the heptanes will be concentrated in the bottoms fraction and subjected to reforming as part of the charge thereto. The hexanes will be recycled to isomerizer 34 by the circuit heretofore described.
  • additional fractionating zones may be provided to split the heptanes into high yoctane low boiling components and low octane high boiling componentsand the separated high boiling heptane fraction may be subjected to isomerization in the ⁇ rarêt saine orjdiffernt nzone vor zenesrrmthat used for "lsomer'izing the pentanes and/or hexan'cs.
  • fractionating zones "2 ⁇ "and 13 will vfunction tseparateiCg CS 'and .C7 from C8 :and heavier compo- "h'ei'its -Thefpentane's'will be separated from vthe hexanes V'iiigzon'e will Acomprise C8 'and heavier.
  • the novelprocess of the --present'invention produces a rhigh ⁇ yield of high octane 4gasoline product, which product iiswithdrawn from the k:process:through line V50.
  • the linalg'asoline product will ,have'a Researchleaded octanenumber above95 and up to 102 or more.
  • Anotheradvantage to the process of thepresentinvention is that the severity of the reforming operation is lower than otherwise would be required to yre ⁇ a ⁇ .ch this high octane product in the absence of the isomerizationfsteps of the process Therefore, the yield obtained in 'thereforming operation is considerably increased and the lie of the reforming catalystis considerably extended.
  • the process of the present invention produces this high octane gasoline product with an increase in yield of 6 Ato 10% or more, over and above that previously attainablc.
  • Example I example illustrates the advantages of the present invention when processing Arabian straight run gasoline hailing a boiling range of from 2 04 u to 362. F., an API gravity of 57.9 and a Research clear octane number of 34. l The octane number of the total gasoline product to b e obtained is 98 Research leaded.
  • the gasoline On lthe basis of charging 10,000 barrelsper day, the gasoline ishsplit into 2,200 barrels per day of C and C6 and 7,800 barrelsper daypf C7 and heavier.
  • the C5 and C6 fraction is further split into 1 ,l00 barrels per day each of a C5 fraction and of a C5 fraction.
  • the Cf; andheavier fraction is subjected to reforming in the presence of a catalyst comprising alumina, about (14% by weight of platinum and about 0.5% by weight of combined halogen, ythe lattercomprising about 0.3% by weightof combined uorineandabout 0.2% by Weight of combined chlorine.
  • the reforming is eiected in a 'series of 3 -catalyst-containing reactors with intervening heating ofthe reactor effluents between reactors.
  • chl'ngewto reforming is introduced into the reaction zone at a Vtemperature of about 895 F., and at a space velocity of about 2.5.
  • the reactors are maintained at a Apressnrebfabout 500 pounds per square inch, and hydrogen is recycled to'mintain a hydrogen to hydrocarbon ratio .
  • catalytic reforming alone is usedV and is severity tofproduce, a ,98 leaded octane number product,
  • Example II 'fln an operation similar to 'thatdescribed in'Ex'ample I but utilizing a Wyoming straight Vrun-gasoline charge and Ioperating to produce'a leaded (Research octane product r(5h97, opierat'ionin accordance with the present invention yields 1,010 ddi'tionl ⁇ birrel ⁇ s-iper dayof 97 ⁇ o'ctane gaso- ⁇ li s'compared to catalytic reforming lalone at a severity 'necessary to achieve Vvtlii's'octarie product.
  • the Wyoming Vstraight run g'e'fsoliri'e has a boiling 'range of 210 to 400 R, 'an 'AEI tvgravity fof 56.4 and "a Research 'clear octane er of 52.5.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US594592A 1956-06-28 1956-06-28 Upgrading gasoline Expired - Lifetime US2905619A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
US594592A US2905619A (en) 1956-06-28 1956-06-28 Upgrading gasoline
GB19947/57A GB809635A (en) 1956-06-28 1957-06-25 Process for upgrading gasoline
DEU4615A DE1057711B (de) 1956-06-28 1957-06-27 Verbundverfahren zur Aufwertung von Benzin
ES0236274A ES236274A1 (es) 1956-06-28 1957-06-27 Un procedimiento completo para mejorar la gasolina.
BE558772A BE558772A (fr) 1956-06-28 1957-06-27 Procédé pour améliorer la qualité de l'essence de pétrole
FR1178064D FR1178064A (fr) 1956-06-28 1957-06-28 Procédé pour améliorer la qualité de l'essence de pétrole
MY57/62A MY6200057A (en) 1956-06-28 1962-12-30 Process for upgrading gasoline

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US594592A US2905619A (en) 1956-06-28 1956-06-28 Upgrading gasoline

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BE (1) BE558772A (fr)
DE (1) DE1057711B (fr)
ES (1) ES236274A1 (fr)
FR (1) FR1178064A (fr)
GB (1) GB809635A (fr)
MY (1) MY6200057A (fr)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2983667A (en) * 1958-12-10 1961-05-09 Socony Mobil Oil Co Inc Process for upgrading petroleum naphthas
US3002917A (en) * 1959-10-01 1961-10-03 Socony Mobil Oil Co Inc Method of making 104-106 r.o.n. leaded gasoline
US3002916A (en) * 1956-09-06 1961-10-03 Socony Mobil Oil Co Inc Two-stage reforming with intermediate fractionation
US3003949A (en) * 1959-06-10 1961-10-10 Socony Mobil Oil Co Inc Process for manufacturing 104-106 r.o.n. leaded gasoline
US3016344A (en) * 1958-08-27 1962-01-09 Houdry Process Corp Upgrading natural gasoline
US3018244A (en) * 1958-12-18 1962-01-23 Kellogg M W Co Combined isomerization and reforming process
US3060116A (en) * 1959-11-06 1962-10-23 Socony Mobil Oil Co Inc Combination reforming and cracking process
US3071535A (en) * 1959-07-06 1963-01-01 Gulf Research Development Co Process for making a low sensitivity premium gasoline
US3131235A (en) * 1960-11-23 1964-04-28 Universal Oil Prod Co Simultaneous isomerization of pentane and hexane with selective fractionation
US3150205A (en) * 1960-09-07 1964-09-22 Standard Oil Co Paraffin isomerization process
US3658690A (en) * 1970-03-13 1972-04-25 Mobil Oil Corp Gasoline upgrading
US3718710A (en) * 1971-06-30 1973-02-27 Texaco Inc Hydrotreating and hydroisomerizing c{11 {11 and c{11 {11 hydrocarbon streams
US4162212A (en) * 1978-08-30 1979-07-24 Chevron Research Company Combination process for octane upgrading the low-octane C5 -C6 component of a gasoline pool
US4181599A (en) * 1978-10-23 1980-01-01 Chevron Research Company Naphtha processing including reforming, isomerization and cracking over a ZSM-5-type catalyst
US4191634A (en) * 1978-10-02 1980-03-04 Chevron Research Company Octane upgrading process for light paraffins using a combination of two palladium-zeolite catalysts
US4647368A (en) * 1985-10-15 1987-03-03 Mobil Oil Corporation Naphtha upgrading process
US20140094632A1 (en) * 2012-09-28 2014-04-03 Uop Llc Methods and apparatuses for recovering normal hexane from reformate streams
FR3020374A1 (fr) * 2014-04-29 2015-10-30 Axens Procede de production d'essence comprenant une etape d'isomerisation suivie d'au moins deux etapes de separation.
CN105820838A (zh) * 2015-01-07 2016-08-03 中国石油化工股份有限公司 一种轻烃异构化方法
WO2020028285A1 (fr) * 2018-07-30 2020-02-06 Uop Llc Procédé intégré de production d'essence
WO2020028369A1 (fr) * 2018-07-30 2020-02-06 Uop Llc Procédé intégré de production d'essence
US11021422B1 (en) 2019-12-04 2021-06-01 Saudi Arabian Oil Company Integrated processes to produce gasoline blending components from light naphtha
RU2772646C1 (ru) * 2019-03-28 2022-05-23 Юоп Ллк Интегрированный процесс для максимального извлечения водорода

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1125102B (de) * 1959-06-26 1962-03-08 Universal Oil Prod Co Verbundverfahren zur Aufwertung von C- und schwerere Kohlenwasserstoffe enthaltendemparaffinischem Benzin
DE1181356B (de) * 1960-07-22 1964-11-12 Shell Int Research Verfahren zur Herstellung von Kohlenwasserstoffmischungen mit hoher Octanzahl

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2443607A (en) * 1943-03-31 1948-06-22 Standard Oil Co Heptane isomerization
US2479110A (en) * 1947-11-28 1949-08-16 Universal Oil Prod Co Process of reforming a gasoline with an alumina-platinum-halogen catalyst
US2698829A (en) * 1950-12-29 1955-01-04 Universal Oil Prod Co Two-stage process for the catalytic conversion of gasoline
US2740751A (en) * 1952-02-23 1956-04-03 Universal Oil Prod Co Reforming of both straight run and cracked gasolines to provide high octane fuels

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2443607A (en) * 1943-03-31 1948-06-22 Standard Oil Co Heptane isomerization
US2479110A (en) * 1947-11-28 1949-08-16 Universal Oil Prod Co Process of reforming a gasoline with an alumina-platinum-halogen catalyst
US2698829A (en) * 1950-12-29 1955-01-04 Universal Oil Prod Co Two-stage process for the catalytic conversion of gasoline
US2740751A (en) * 1952-02-23 1956-04-03 Universal Oil Prod Co Reforming of both straight run and cracked gasolines to provide high octane fuels

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3002916A (en) * 1956-09-06 1961-10-03 Socony Mobil Oil Co Inc Two-stage reforming with intermediate fractionation
US3016344A (en) * 1958-08-27 1962-01-09 Houdry Process Corp Upgrading natural gasoline
US2983667A (en) * 1958-12-10 1961-05-09 Socony Mobil Oil Co Inc Process for upgrading petroleum naphthas
US3018244A (en) * 1958-12-18 1962-01-23 Kellogg M W Co Combined isomerization and reforming process
US3003949A (en) * 1959-06-10 1961-10-10 Socony Mobil Oil Co Inc Process for manufacturing 104-106 r.o.n. leaded gasoline
US3071535A (en) * 1959-07-06 1963-01-01 Gulf Research Development Co Process for making a low sensitivity premium gasoline
US3002917A (en) * 1959-10-01 1961-10-03 Socony Mobil Oil Co Inc Method of making 104-106 r.o.n. leaded gasoline
US3060116A (en) * 1959-11-06 1962-10-23 Socony Mobil Oil Co Inc Combination reforming and cracking process
US3150205A (en) * 1960-09-07 1964-09-22 Standard Oil Co Paraffin isomerization process
US3131235A (en) * 1960-11-23 1964-04-28 Universal Oil Prod Co Simultaneous isomerization of pentane and hexane with selective fractionation
US3658690A (en) * 1970-03-13 1972-04-25 Mobil Oil Corp Gasoline upgrading
US3718710A (en) * 1971-06-30 1973-02-27 Texaco Inc Hydrotreating and hydroisomerizing c{11 {11 and c{11 {11 hydrocarbon streams
US4162212A (en) * 1978-08-30 1979-07-24 Chevron Research Company Combination process for octane upgrading the low-octane C5 -C6 component of a gasoline pool
US4191634A (en) * 1978-10-02 1980-03-04 Chevron Research Company Octane upgrading process for light paraffins using a combination of two palladium-zeolite catalysts
US4181599A (en) * 1978-10-23 1980-01-01 Chevron Research Company Naphtha processing including reforming, isomerization and cracking over a ZSM-5-type catalyst
US4647368A (en) * 1985-10-15 1987-03-03 Mobil Oil Corporation Naphtha upgrading process
US20140094632A1 (en) * 2012-09-28 2014-04-03 Uop Llc Methods and apparatuses for recovering normal hexane from reformate streams
FR3020374A1 (fr) * 2014-04-29 2015-10-30 Axens Procede de production d'essence comprenant une etape d'isomerisation suivie d'au moins deux etapes de separation.
WO2015165763A1 (fr) * 2014-04-29 2015-11-05 Axens Procede de production d'essence comprenant une etape d'isomerisation suivie d'au moins deux etapes de separation
CN105820838A (zh) * 2015-01-07 2016-08-03 中国石油化工股份有限公司 一种轻烃异构化方法
CN105820838B (zh) * 2015-01-07 2017-10-03 中国石油化工股份有限公司 一种轻烃异构化方法
WO2020028285A1 (fr) * 2018-07-30 2020-02-06 Uop Llc Procédé intégré de production d'essence
WO2020028369A1 (fr) * 2018-07-30 2020-02-06 Uop Llc Procédé intégré de production d'essence
RU2753530C1 (ru) * 2018-07-30 2021-08-17 Юоп Ллк Интегрированный способ производства бензина
RU2753968C1 (ru) * 2018-07-30 2021-08-24 Юоп Ллк Интегрированный способ производства бензина
RU2772646C1 (ru) * 2019-03-28 2022-05-23 Юоп Ллк Интегрированный процесс для максимального извлечения водорода
US11021422B1 (en) 2019-12-04 2021-06-01 Saudi Arabian Oil Company Integrated processes to produce gasoline blending components from light naphtha

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MY6200057A (en) 1962-12-31
BE558772A (fr) 1960-04-08
FR1178064A (fr) 1959-05-04
GB809635A (en) 1959-02-25
ES236274A1 (es) 1958-03-01
DE1057711B (de) 1959-05-21

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