Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/42—Platinum
• • H—ELECTRICITY
  • H04—ELECTRIC COMMUNICATION TECHNIQUE
  • H04H—BROADCAST COMMUNICATION
  • H04H20/00—Arrangements for broadcast or for distribution combined with broadcast
  • H04H20/86—Arrangements characterised by the broadcast information itself
  • H04H20/88—Stereophonic broadcast systems
• • H—ELECTRICITY
  • H04—ELECTRIC COMMUNICATION TECHNIQUE
  • H04J—MULTIPLEX COMMUNICATION
  • H04J1/00—Frequency-division multiplex systems
• • H—ELECTRICITY
  • H04—ELECTRIC COMMUNICATION TECHNIQUE
  • H04S—STEREOPHONIC SYSTEMS 
  • H04S1/00—Two-channel systems
  • H04S1/002—Non-adaptive circuits, e.g. manually adjustable or static, for enhancing the sound image or the spatial distribution
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/03—Precipitation; Co-precipitation
• • 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
  • C10G2400/02—Gasoline

Definitions

• This invention relates to a process for the purification be practically free from aromatic hydrocarbons and other impurities, namely s'ulphur containing compounds,
• aromatic hydrocarbons and other impurities namely s'ulphur containing compounds
• the use" of unleaded gasoline results in an increasing demand for branched paraffinic hydrocarbons, some of these compounds having a. particularly high octane number. Therefore, it is desirable to isomerizethe straight chain parafiinsagf these light parafiinic fractions or, at
• the process of the present invention is applied to lighter fractions and it must perform to practically completely remove the aromatic hydrocarbons and also the sulphur-containing compounds. Therefore the present process differs from the prior processes in that a specific feed is treated in the presence of a specific catalyst in order to obtain a product which must have specified properties.
• the feed to the present process mainly comprises parafiinichydrocarbons containing from 5 to 7 carbon atoms inclusive, more generally 5 to 6 carbon atoms, the amount of straight-chain paraffins being at least 30% and more often at least 50%.by weight.
• the feed contains also b ranched paraflins and cycloparatfins.
• the amount of aromatic hydrocarbons, more particularly benzene and toluene, may be present within wide limits, but generally is present in an amount within the range of 0.1 and 10% by weight.
• the amount of sulphur-containing compounds present in the feed to the process of the presentin-vention genv is between about 50 and 500 ppm. If ,the amount -.is higher, the parafilnic fraction is advantageously desulphurized prior to use in the present process. This desulphurization treatment need not be directed in such a manner'as to secure a complete removal of the sulphurcontaining compoundsas required with prior processes.
• a caustic wash will likely suffice.
• Another means of such desulphurization comprises subjecting said petroleum cut to a sweetening treatment to convert mercaptans contained in said out into heavier disulphides so that a subsequent distillation gives a parafiinic fraction with a low sulphur content.
• the object of these desulphurizing treatments is only to reduce the sulphur content of the paraflinic fraction to a level lower than about 500 ppm.
• the prior processes generally require a complete removal of the sulphur-containing compounds before hydrogenationof the parafiinic fraction and therefore, are more expensive.
• the light parafline fraction is hydrogenated under the above specified conditions, preferably, however, hydrogenation is carried out at a temperature within the range of 175 to 325 C., under a partial pressure of hydrogen of between about to 75 kg/cm. and with a space velocity from 0.5 to 20.
• the optimum conditions depend not only On the composition of the parafiinic fraction and on its content of aromatic hydrocarbons, cycloparaffinic hydrocarbons and sulphur-containing compounds, but they depend also on each other. Therefore, the temperature to be applied for a substantially complete removal of the aromatic hydrocarbons varies as a function of the sulphur content of the feed, the other conditions remaining equal. Also, the temperature may be lowered when the pressure is higher. Determination of such optimum value within the above defined ranges may readily be made by those skilled in the art.
• the hydrogenating catalyst will contain from 0.1 to 2% by weight of platinum on a silica-alumina carrier, where silica is in major quantity and where at least 30% of the platinum is distributed on the catalyst surface which is accessible to the reactants. Indeed, it has been found that with catalysts, whose carrier does not contain .a greater amount of silica than alumina or whose platinum is poorly distributed onthe surface, the degree of aromatic hydrogenation is lower under the conditions which prevail than with the catalyst utilized in the present invention.
• a convenient process for preparing the present catalyst comprises impregnating the silica-alumina carrier with a solution of a platinum copound, usually chloroplatinic acid and then evaporating the solution and thereafter drying and calcinating the catalyst at about 400 C.
• wpregnation of the carrier may be performed with solutions of water soluble platinum salts, but with the use of solutions having a pH from about 1 to 7.
• An extended drying and a moderate calcination of the catalyst are particularly suitable. Under these conditions, at least 30% of the platinum is distributed on the total surface of the catalyst which is accessible to the reactants. Determination of this percentage of platinum on the surface is carried out by using described methods, e.g. the method of D. E. Mears and R. C. Hansford, in Journal of Catalysis, vol. 9, pp. 125-127 (1967).
• n-Pentane 61.0 Iso-pentane 13.8 Cy'clopentane 4.7 2.2-dimethylbutane 0.6 2.3-dimethylbutane 0.4 Z-methylpentane I I 3.5 3-rnethylpentane 3.3 n-Hexane 8.2 Methylcyclopentane 3.0
• the operating conditions for hydrogenation were the following:
• the catalyst used in each test consisted of platinum on a silica-alumina carrier. However, the ratios of silica, alumina and platinum were ditferent in each test. The catalyst compositions and the results of these tests are summarized in Table I.
• a catalyst carrier which has a lower content in silica (test 1) does not perform an adequate hydrogenation, although the content and the distribution of the platinum are substantially the same as those of the catalysts of tests 2 and 3. The same appears with a catalyst having a poor distribution of the platinum (test 4) or with a catalyst having a low content in platinum (test 5).
• composition of the used light paraflinic'frac'tion hydrogenated was as follows:
• the hydrogenated products were distilled to remove H S formed during the hydrogenation.
• the aromatic hydrocarbons of a light paraffinic fraction may befhydrogenated with a practically quantitative yield; Thebest results are obtained when the sulphur content of the feed is not higher than p.p.m.
• the hydrogenation preferably is carried out at a temperature between 275 and 330 C. and under a partial pressure of hydrogen varying between about 50 and 70 kg./ cm. and with the hydrogenation yield higher than 99.5%.
• the sulphur-containing compounds are simultaneously converted into His, which is easily distilled off, so that the end product is practically sulphur-free.
• the hydrogenated fraction does not contain more than 100 p.p.m. of residual aromatics and not more than 30 p.p.m. of sulphur, in order to prevent rapid deactivation of the isomerization catalyst.
• a hydrogenating catalyst consisting essentially of between 0.1 and 2% of platinum on a silica-alumina carrier, silica being in major quantity, and at least 30% of the platinum being distributed on the catalyst surface which is accessible to the reactants, fractionating the products of the hydrogenation to separate the hydrogenated sulfurand nitrogen-conta" ining compounds and to recover a paraflinic fraction substantially containing only parafiinic hydrocarbons with an increased content of cycloparatllns, less than 100 p.p.m. aromatic hydrocarbons and less than 30 p.p.m. sulphur.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Signal Processing (AREA)
• Materials Engineering (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Physics & Mathematics (AREA)
• Acoustics & Sound (AREA)
• Computer Networks & Wireless Communication (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Applications Claiming Priority (1)

Publications (1)

Family

ID=3857685

Family Applications (1)

Country Status (10)

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• 1971
  • 1971-02-05 BE BE762565A patent/BE762565A/xx unknown
  • 1971-05-29 ES ES391725A patent/ES391725A1/es not_active Expired
  • 1971-06-01 FR FR7119714A patent/FR2124207B1/fr not_active Expired
  • 1971-07-06 GB GB3163771A patent/GB1351507A/en not_active Expired
  • 1971-07-14 NL NL154549D patent/NL154549C/nl active
  • 1971-07-14 NL NL717109696A patent/NL154549B/xx not_active IP Right Cessation
  • 1971-09-13 DE DE2145639A patent/DE2145639C3/de not_active Expired
  • 1971-10-18 US US00190386A patent/US3827974A/en not_active Expired - Lifetime
  • 1971-10-19 CA CA125,492A patent/CA960173A/en not_active Expired
  • 1971-12-02 AU AU36384/71A patent/AU463422B2/en not_active Expired
  • 1971-12-10 JP JP46099591A patent/JPS5017203B1/ja active Pending

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