US2852442A - Catalytic reforming of petroleum hydrocarbons - Google Patents

Catalytic reforming of petroleum hydrocarbons Download PDF

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Publication number
US2852442A
US2852442A US609146A US60914656A US2852442A US 2852442 A US2852442 A US 2852442A US 609146 A US609146 A US 609146A US 60914656 A US60914656 A US 60914656A US 2852442 A US2852442 A US 2852442A
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United States
Prior art keywords
catalytic reforming
sulphur dioxide
aromatic
raffinate
product
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Expired - Lifetime
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US609146A
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English (en)
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Moy John Arthur Edgar
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BP PLC
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BP PLC
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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
    • 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
    • C10G21/08—Inorganic compounds only
    • C10G21/10—Sulfur dioxide
    • 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
    • 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
    • C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
    • C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
    • C10G61/04—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only the refining step being an extraction

Definitions

  • This invention relates to the catalytic reforming process which, as applied to petroleum hydrocarbons, consists in contacting the hydrocarbons at elevated temperature and pressure with a catalyst for the various chemical reactions which contribute to the production of aromatics whereby a product of increased aromatic content as cornpared with the feedstock is obtained.
  • the catalytic reforming process is particularly useful in the petroleum industry for treating naphtha fractions of low aromatic content and low octane number for the production of naphthas having increased aromatic content and higher octane number and therefore more suitable for use as motor gasolines.
  • One such process which has been developed is the Platforming process in which a catalyst is used comprising a small amount of platinum, and sometimes a halogen, supported on an alumina base.
  • a catalyst comprising a small amount of platinum, and sometimes a halogen, supported on an alumina base.
  • the present invention relates to a process of this latter kind and has among its objects to obtain a product having an aromatic content of 70-80%
  • the process according to the present invention comprises contacting a catalytic reformer feedstock with liquid sulphur dioxide in conventional manner for the production of an aromatic extract and a raffinate, passing the -ratlnate to a catalytic reforming zone for the production of aromatics, contacting the product from the catalytic reforming zone with liquid sulphur dioxide in conventional manner for the production of an aromatic extract of the same aromatic content as the aromatic extract previously referred to, and a rainate, and passing the rafnate to the catalytic reforming zone together with the rainate previously referred to.
  • Extraction of aromatics from the naphtha feedstock is advantageous for two reasons: (a) an increased quantity of aromatics can be formed by increased dehydrocyclization of parains, (b) there is a reduction in quantity of unreactive compounds passing through the catalytic reforming process.
  • Extraction of aromatics from the catalytic reformate is a more eiective method of obtaining a iinal product of the required aromatic content than is the operation of the catalytic reforming process at higher severity which would result in rapid deactivation of the catalyst.
  • the production of aromatic extracts of the same aromatic content may be accomplished by operating at the same temperature but with different solvent to oil ratios. This method of operation has the following advantages:
  • the two extraction towers can be made as one column with two compartments.
  • a product of still greater aromatic content may be obtained according to a further feature of the invention component and recycled to the extraction towers.
  • the feedstock for example a naphtha boiling in the range 90 to 190 C. and containing 12 to 20% aromatics
  • a conventional multistage solvent extraction tower A at a temperature in the range 30 to
  • liquid sulphur dioxide in the proportion of 50 to 150 volu-rnes of sulphur dioxide per volumes of naphtha.
  • the solvent ratio is adjusted to give an extract containing the required concentration of aromatics.
  • the products from this operation are raffinate phase l and extract phase l.
  • Raflinate phase l is combined with raffinate phase 2 (as described below) and is passed to a raffinate phase evaporating system C where sulphur dioxide is removed from the substantially aromatic-free naphtha by distillation. tower.
  • the aromatic-free naphtha is passedto a catalytic -rei forming process D in which a product containing about 40 to 50% aromatics is made.
  • the stabilized reformate is passed to a second conventional multistage solvent extraction tower B in which it is contacted countercurrently at a temperature in the range 30 to +20 F. with liquid sulphur dioxide in the proportion of 200 to 400 volumes of sulphur dioxide per 100 volumes of reformate.
  • the solvent ratio is adjusted to give an extract containing the required concentration of aromatics which is the same concentration as that obtained from the first extraction operation.
  • the products from this operation are ranate phase 2 and extract phase 2.
  • Raflinate phase 2 is combined with rainate phase l (as described above) before passing to the ratlinate phase evaporators C in which sulphur dioxide is removed from the substantially aromatic-free naphtha which is recycled (with the dearomatized naphtha feedstock) to the reforming process.
  • Extract phase 2 is combined with extract phase 1 before passing to the extract phase evaporating system E where sulphur dioxide is removed from the hydrocarbon
  • the hydrocarbon component is the desired product containing 70% to 80% aromatics.
  • Rainate phase 3 is passed to an evaporating system G where sulphur dioxide is distilled off and recycled to the extraction towers A and B, while the hydrocarbon part of the ratllnate phase is fed to a ratlinate splitter H.
  • the splitter will give material in the naphtha boiling range as an overhead product which is recycled to the extraction tower A, and kerosine as a bottoms product which is recycled to the wash tower F.
  • Extract phase 3 A is passed to an evaporating system I Where sulphur dioxide is distilled off and recycled to extraction towers A and B, while the hydrocarbon part of the extract phase is fed to an extract splitter K.
  • the splitter will give as an overhead product the required product containing 95% aromatics, and kerosine as a bottoms product which is recycled to the Wash tower F.
  • a process for the catalytic reforming of a petroleum feedstock which comprises contacting the feedstock with liquid sulphur dioxide for the production of an aromatic extract and a ranate, passing the rai'linate Vto a catalytic reforming zone for the production of aromatics, contacting the product from the catalytic reforming zone with liquid sulphur dioxide for the production of an aromatic extract and a raffinate, the contacting of the feedstock and the contacting of the product of the catalytic reforming zone with liquid sulphur dioxide being carried out at the same temperature but with different solvent to oil ratios to give aromatic extracts of the same aromatic content, and passing the raflinate to the catalytic reforming zone together with the rafnate previously referred to.
  • a process for the catalytic reforming of a petroleum feedstock which comprises contacting the feedstock with liquid sulphur dioxide for the production of an aromatic extract and a ratiinate, passing the raiiinate to a catalytic reforming zone for the production of aromatics, 'contacting the product from the catalytic reforming zone with liquid sulphur dioxide for the production of an aromatic extract of the same aromatic content as the aromatic extract previously referred to, passing the ratnate to the catalytic reforming zone together with the raffinate previously referred to, combining said aromatic extracts, contacting the combined extracts, in solution in liquid sulphur dioxide, countercurrently with a dearomatised heavy kerosine fraction, the ratio of said kerosine fraction to the hydrocarbons in the combined extracts being in the range of 0.25 to 1.5 :1 by volume, and distilling the extracts after being thus contacted for the recovery of a product of increased aromatic content.

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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)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US609146A 1955-09-23 1956-09-11 Catalytic reforming of petroleum hydrocarbons Expired - Lifetime US2852442A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB27186/55A GB800430A (en) 1955-09-23 1955-09-23 Improvements relating to the catalytic reforming of petroleum hydrocarbons

Publications (1)

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US2852442A true US2852442A (en) 1958-09-16

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US609146A Expired - Lifetime US2852442A (en) 1955-09-23 1956-09-11 Catalytic reforming of petroleum hydrocarbons

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US (1) US2852442A (en(2012))
BE (1) BE550984A (en(2012))
DE (1) DE1062862B (en(2012))
FR (1) FR1156734A (en(2012))
GB (1) GB800430A (en(2012))

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3193489A (en) * 1962-09-13 1965-07-06 Phillips Petroleum Co Solvent extraction process
US4956052A (en) * 1986-02-28 1990-09-11 Suntory Limited Process for separation using supercritical fluid

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2350834A (en) * 1941-06-18 1944-06-06 Texas Co Conversion of hydrocarbons
US2379334A (en) * 1941-11-08 1945-06-26 Texas Co Manufacture of motor fuel
US2724682A (en) * 1951-12-21 1955-11-22 Phillips Petroleum Co Sulfur dioxide extraction process
US2727848A (en) * 1953-06-08 1955-12-20 American Oil Co Solvent recovery in solvent extraction

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA368090A (en) * 1937-08-17 Henshaw Arveson Maurice Hydrocarbon oil treatment
US2146039A (en) * 1935-11-29 1939-02-07 Standard Oil Dev Co Method of improving naphtha
NL45184C (en(2012)) * 1936-03-30
US2249461A (en) * 1937-08-17 1941-07-15 Standard Oil Co Manufacture of antiknock gasoline
US2132365A (en) * 1937-12-18 1938-10-04 Texas Co Treatment of hydrocarbons
US2241430A (en) * 1938-02-07 1941-05-13 Standard Oil Co California Process of treating hydrocarbons
US2522696A (en) * 1947-06-27 1950-09-19 Sinclair Refining Co Catalytic conversion of naphtha for the production of high antiknock gasoline

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2350834A (en) * 1941-06-18 1944-06-06 Texas Co Conversion of hydrocarbons
US2379334A (en) * 1941-11-08 1945-06-26 Texas Co Manufacture of motor fuel
US2724682A (en) * 1951-12-21 1955-11-22 Phillips Petroleum Co Sulfur dioxide extraction process
US2727848A (en) * 1953-06-08 1955-12-20 American Oil Co Solvent recovery in solvent extraction

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3193489A (en) * 1962-09-13 1965-07-06 Phillips Petroleum Co Solvent extraction process
US4956052A (en) * 1986-02-28 1990-09-11 Suntory Limited Process for separation using supercritical fluid

Also Published As

Publication number Publication date
GB800430A (en) 1958-08-27
FR1156734A (fr) 1958-05-20
DE1062862B (de) 1959-08-06
BE550984A (en(2012))

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