US3635815A - Process for producing a mixture of high-purity c{11 aromatic hydrocarbons - Google Patents

Process for producing a mixture of high-purity c{11 aromatic hydrocarbons Download PDF

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Publication number
US3635815A
US3635815A US838619A US3635815DA US3635815A US 3635815 A US3635815 A US 3635815A US 838619 A US838619 A US 838619A US 3635815D A US3635815D A US 3635815DA US 3635815 A US3635815 A US 3635815A
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fraction
purity
aromatic hydrocarbons
zone
reformate
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Paul J Kuchar
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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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
    • C10G7/00—Distillation of hydrocarbon oils

Definitions

  • a TTOR/VEYS PROCESS FOR PRODUCING A MIXTURE OF HIGH- PURITY C AROMATIC HYDROCARBONS BACKGROUND OF THE INVENTION This invention relates to a process for producing a mixture of high purity C aromatic hydrocarbons. It particularly relates to a process for producing a mixture of high-purity C aromatic hydrocarbons having an aromatic hydrocarbon purity of greater than 98 liquid volume percent.
  • the present invention provides a process for producing a mixture of high-purity C aromatic hydrocarbons which comprises the steps of: (a) introducing a C -400 F. naphtha feed fraction into a feed splitter prefractionation zone; (b) splitting said fraction into an overhead fraction having a 270 F. to 275 F. end point and a bottoms fraction having a higher end point; endpoint c) introducing said overhead fraction having a 270 endpoint; to 275 F.
  • the essence of my invention comprises tying in end point control of the overhead fraction leaving the feed splitter prefractionation zone and the nonaromatic content of the reformate charge to the severity of the reforming operation as measured by the reformate target octane number or the temperature at which the reforming zone is maintained at a given space velocity.
  • a naphtha containing feed is passed via line 1 into crude tower 2 which is a conventional crude tower such as is found in any typical refinery complex.
  • crude tower 2 which is a conventional crude tower such as is found in any typical refinery complex.
  • a C 400" F. naphtha feed fraction is removed from crude tower 2 via sidecut means 5 via line 6 and passed into a feed splitter prefractionation zone 7. Hydrocarbons lighter than the C 400" F. naphtha will be removed from crude tower 2 via line 3 and heavier hydrocarbons removed from tower 2 via line 4.
  • the feed splitter prefractionation zone 7 is operated so that an overhead fraction having a 270 F. to 275 F. endpoint is separated from a bottoms fraction having a higher end point.
  • the feed splitter will operate at a bottoms temperature of 300 F. to 400 F. and the bottoms fraction is removed from feed splitter 7 via line 8 and passed to a heavy motor fuel reformer (not shown).
  • the overhead fraction having a 270 F. to 275 F. endpoint is passed via line 9 into catalytic reforming zone which is maintained under reforming conditions sufficient to produce a reformate having a minimum of C hydrocarbon. It has been found that when the overhead fraction having a 270 F. to 275 F.
  • the reforming conditions shall include a C reformate clear target octane of from 92.0 to 96.0.
  • the reforming conditions shall include a C reformate clear target octane of greater than 100.0.
  • the reforming zone may contain any suitable reforming catalyst known in the art including those catalysts comprising refractory inorganic oxides such as alumina, which are-combined with at least one metal from Group VIII of the Periodic Table and, if desired, a halogen component as well as those reforming catalysts utilizing a crystalline aluminosilicate as the catalyst support.
  • Reforming conditions include a temperature in the range of from 800 F. to 1,100 F. or more, and preferably a temperature in the range of from 850 F. to 1,050 F., and a pressure in the range of from 50 p.s.i.g. to about 1,000 p.s.i.g.
  • the reforming zone may be maintained at a liquid hourly space velocity of 0.1 to 20.0 or more, and preferably in the range of from about 0.5 to 15.0 or more, and a gaseous liquid hourly space velocity in the range of from 100 to about 3,000 or more. It is further apparent to one skilled in the art that the 270 F. to 275 F. endpoint overhead feed fraction may be passed through the reforming zone in an upward, downward or radial manner.
  • the reformate passes from reforming zone 10 via line 11 into a deoctanizer zone 12 wherein a C naphthene and lighter hydrocarbon fraction is separated from a C aromatic and heavier hydrocarbon fraction.
  • the deoctanizer may be a conventional fractional distillation column and is usually maintained at a pressure of about p.s.i.g. and a bottoms temperature of from about 300 F. to about 350 F. The top temperature is maintained in the range of from about 200 F. to about 300 F.
  • the C naphthene and lighter hydrocarbon fraction is passed from deoctanizer 12 via line 13 to a motor fuel blending facility (not shown).
  • the C aromatic and heavier hydrocarbon fraction is then passed from deoctanizer 12 via line 14 into a rerun column zone 15 wherein a mixture of highpurity C aromatic hydrocarbons is separated from a C hydrocarbon fraction.
  • the high purity C aromatic hydrocarbons are represented as being removed from the rerun column via line 17.
  • the C hydrocarbon fraction is removed from the rerun column via line 16.
  • C -lhydrocarbon fraction is removed from the rerun column via line 16.
  • C fractions find use as a heavy aromatic solvent and may be utilized for motor fuel blending.
  • feed treating means (not shown) be placed in such a manner that, for example, the C -400 F. naphtha feed fraction passing via line 6 into feed splitter prefractionation zone 7 be passed through the treating zone for removal of various impurities that may be present.
  • a feed treating zone may also be located in line 9 between the feed splitter prefractionation zone and the reforming zone for removal of impurities from this fraction prior to the fraction passing into the catalytic reforming zone.
  • Feed compound impurities that may be removed include sulfur compound impurities, nitrogen compound impurities, oxygenated compound impurities, and heavy metal impurities that may be present in a conventional naphtha feed.
  • this invention provides a process for producing a mixture of highpurity C aromatic hydrocarbons having a aromatic hydrocarbon purity of greater than 98 liquid volume percent which comprises the steps of: (a) introducing a sidecut fraction from a crude unit distillation column comprising a C -400 F. naphtha into a treating zone containing a means for removing sulfur and nitrogen compound impurities from said fraction; (b) removing from said treating zone a treated C -400 F. naphtha feed fraction and introducing said fraction into a feed splitter prefractionation zone; (0) introducing said overhead fraction having a 270 F. to 275 F.
  • the present invention provides a process for producing a mixture of C aromatic hydrocarbons utilizing a process comprising fractionation and catalytic reforming exclusive of extraction. It was found that it was essential to prefractionate the reformate charge to at most 270 F. to 275 F. .endpoint (ASTM) inasmuch as experimentation showed that reformates with a clear target octane of 94 to 102 which were produced from naphthas with an end point of 275 F. to 280 F., when fractionated to separate a 275 F.297 F. xylene heartcut, yielded C aromatic hydrocarbon purities of less than 94 percent and purities as low as 88 liquid volume C aromatic hydrocarbons.
  • a process for producing a mixture of C aromatic hydrocarbons having an aromatic hydrocarbon purity of greater than 98 liquid volume percent by fractional distillation and catalytic reforming, exclusive of extraction which comprises the steps of:
  • said naphtha fraction having a 270 F. to 275 F. endpoint comprises from 2 to 5 liquid volume percent C naphthenes plus paraffins and wherein said reforming conditions include a severity producing C reformate clear target octane of from 92.0 to 96.0.
  • said naphtha fraction having a 270 F. to 275 F. endpoint comprises from 5 to 10 liquid volume percent Cg+ naphthenes plus paraffins and wherein said reforming conditions include a severity producing C reformate clear target octane of from 96.0 to 100.0.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US838619A 1969-07-02 1969-07-02 Process for producing a mixture of high-purity c{11 aromatic hydrocarbons Expired - Lifetime US3635815A (en)

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US83861969A 1969-07-02 1969-07-02

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JP (1) JPS547777B1 (en))
CA (1) CA928327A (en))
ES (1) ES381332A1 (en))
FR (1) FR2050451B1 (en))
GB (1) GB1304773A (en))
NL (1) NL7009786A (en))
SU (1) SU365897A3 (en))
ZA (1) ZA704442B (en))

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2401124A1 (fr) * 1977-08-24 1979-03-23 Cosden Technology Procede de production de composes aromatiques de purete elevee
US4174270A (en) * 1977-11-03 1979-11-13 Cosden Technology, Inc. High severity process for the production of aromatic hydrocarbons
US4174271A (en) * 1977-11-03 1979-11-13 Cosden Technology, Inc. High severity reforming
US4808298A (en) * 1986-06-23 1989-02-28 Amoco Corporation Process for reducing resid hydrotreating solids in a fractionator
US6602404B2 (en) * 1997-10-30 2003-08-05 Exxon Mobil Chemical Patents Inc. Process for naphtha reforming
RU2254356C1 (ru) * 2004-02-27 2005-06-20 Открытое акционерное общество "Салаватнефтеоргсинтез" Способ выделения ароматического сольвента, бензола, толуола и высокооктанового компонента бензина с улучшенными экологическими характеристиками из катализатов бензинового и бензольно-толуольного риформинга
RU2255957C1 (ru) * 2004-02-27 2005-07-10 Открытое акционерное общество "Салаватнефтеоргсинтез" Способ выделения о-ксилольного концентрата, бензола, толуола и высокооктанового компонента бензина с улучшенными экологическими характеристиками из катализатов бензинового и бензольно-толуольного риформинга
US10487269B2 (en) * 2013-06-24 2019-11-26 Fluor Technologies Corporation Multiple preflash and exchanger (MPEX) network system for crude and vacuum units

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2653175A (en) * 1951-05-04 1953-09-22 Sun Oil Co Preparation of aromatic hydrocarbons
US3069351A (en) * 1959-07-17 1962-12-18 Socony Mobil Oil Co Inc Utilization of reformer make gas
US3384570A (en) * 1967-02-06 1968-05-21 Phillips Petroleum Co Fractionation and conversion of a naphtha fraction
US3499945A (en) * 1967-06-14 1970-03-10 Sun Oil Co Producing high purity toluene from petroleum naphtha
US3540996A (en) * 1968-08-01 1970-11-17 Mobil Oil Corp Split feed naphtha reforming

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2653175A (en) * 1951-05-04 1953-09-22 Sun Oil Co Preparation of aromatic hydrocarbons
US3069351A (en) * 1959-07-17 1962-12-18 Socony Mobil Oil Co Inc Utilization of reformer make gas
US3384570A (en) * 1967-02-06 1968-05-21 Phillips Petroleum Co Fractionation and conversion of a naphtha fraction
US3499945A (en) * 1967-06-14 1970-03-10 Sun Oil Co Producing high purity toluene from petroleum naphtha
US3540996A (en) * 1968-08-01 1970-11-17 Mobil Oil Corp Split feed naphtha reforming

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2401124A1 (fr) * 1977-08-24 1979-03-23 Cosden Technology Procede de production de composes aromatiques de purete elevee
US4203826A (en) * 1977-08-24 1980-05-20 Cosden Technology, Inc. Process for producing high purity aromatic compounds
US4174270A (en) * 1977-11-03 1979-11-13 Cosden Technology, Inc. High severity process for the production of aromatic hydrocarbons
US4174271A (en) * 1977-11-03 1979-11-13 Cosden Technology, Inc. High severity reforming
US4808298A (en) * 1986-06-23 1989-02-28 Amoco Corporation Process for reducing resid hydrotreating solids in a fractionator
US6602404B2 (en) * 1997-10-30 2003-08-05 Exxon Mobil Chemical Patents Inc. Process for naphtha reforming
RU2254356C1 (ru) * 2004-02-27 2005-06-20 Открытое акционерное общество "Салаватнефтеоргсинтез" Способ выделения ароматического сольвента, бензола, толуола и высокооктанового компонента бензина с улучшенными экологическими характеристиками из катализатов бензинового и бензольно-толуольного риформинга
RU2255957C1 (ru) * 2004-02-27 2005-07-10 Открытое акционерное общество "Салаватнефтеоргсинтез" Способ выделения о-ксилольного концентрата, бензола, толуола и высокооктанового компонента бензина с улучшенными экологическими характеристиками из катализатов бензинового и бензольно-толуольного риформинга
US10487269B2 (en) * 2013-06-24 2019-11-26 Fluor Technologies Corporation Multiple preflash and exchanger (MPEX) network system for crude and vacuum units

Also Published As

Publication number Publication date
NL7009786A (en)) 1971-01-05
ES381332A1 (es) 1972-12-01
GB1304773A (en)) 1973-01-31
FR2050451B1 (en)) 1973-02-02
JPS547777B1 (en)) 1979-04-10
FR2050451A1 (en)) 1971-04-02
DE2032458A1 (de) 1971-01-14
ZA704442B (en) 1971-03-31
CA928327A (en) 1973-06-12
SU365897A3 (en)) 1973-01-08

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Owner name: UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:KATALISTIKS INTERNATIONAL, INC., A CORP. OF MD;REEL/FRAME:005006/0782

Effective date: 19880916

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Owner name: UOP, A GENERAL PARTNERSHIP OF NY, ILLINOIS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:UOP INC.;REEL/FRAME:005077/0005

Effective date: 19880822