| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 141 | PROCESS FOR THE HYDROCRACKING OF HYDROCARBON OILS WITH CATALYSTS HAVING A HIGH FLUORINE CONTENT | CA73356 | 1970-01-28 | CA940860A | 1974-01-29 | T HART MARIUS; DE RUITER HENDRIKUS; PAUL CORNELIS J |
| 142 | PROCESS FOR THE HYDROCRACKING OF HYDROCARBON OILS | GB2047371 | 1971-04-19 | GB1343612A | 1974-01-16 | |
| 1343612 Hydrocracking SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 19 April 1971 [29 Jan 1970] 20473/71 Addition to 1092400 Heading C5E The process of the parent Specification is carried out in two stages, the feed to the second stage having a nitrogen content between 25 and 150 p.p.m. (wt.). The nitrogen content may be adjusted by varying the temperature of the first hydrocracking stage, or by varying the proportion of material recycled from the second cracking stage. Preferably the effluents from both hydrocracking stages are mixed and fractionated, fractions boiling below 350 C. being taken off as product and the residue providing the feed to the second hydrocracking stage. The catalyst in both stages is of the kind specified in the parent Specification, preferably the same catalyst is used in both. The fluorine content of the catalyst may be maintained by adding fluorine to the feed as in Specification 1,104,409. | ||||||
| 143 | FR2035898B1 - | FR7010503 | 1970-03-24 | FR2035898B1 | 1973-03-16 | |
| 144 | A catalyst for hydrocarbon conversion | DE2238044 | 1972-08-02 | DE2238044A1 | 1973-03-08 | ENGELHARD PHILIPPE; WEISANG JOSEPHEDOUARD |
| 145 | DE2034693A1 - | DE2034693 | 1970-07-13 | DE2034693A1 | 1971-02-04 | |
| 146 | SE1113865 | 1965-08-26 | SE326516B | 1970-07-27 | TUPMAN K; IRVING D | |
| 147 | Process for hydro catalytic treatment of alkylaromatics | DE1443470 | 1963-02-16 | DE1443470A1 | 1969-01-30 | GEORGE GOBLE ANTHONY; TUPMAN KENNETH |
| 148 | A process for the conversion of hydrocarbons | DE1443441 | 1962-07-02 | DE1443441A1 | 1968-11-14 | GEORGE GOBLE ANTHONY; VINCENT FLETCHER JOHN |
| 149 | Processes for the hydrogenating cleavage of Kohlenwasserstoffoelen | DES0094272 | 1964-11-20 | DE1242312B | 1967-06-15 | BITTNER CLARENCE WALTER |
| 150 | PROCEDIMIENTO PARA HIDROCRAQUEAR ACEITES HIDROCARBONADOS. | ES325385 | 1966-04-12 | ES325385A1 | 1967-05-01 | |
| 151 | NL6504682A - | NL6504682 | 1965-04-13 | NL6504682A | 1966-10-14 | |
| 152 | BE678510A - | BE678510D | 1966-03-25 | BE678510A | 1966-09-26 | |
| 153 | Improvements relating to the catalytic treatment of alkyl aryl hydrocarbons | GB738962 | 1962-02-26 | GB1023211A | 1966-03-23 | |
| The isomerization of alkyl aryl hydrocarbons having 8 carbon atoms per molecule, while reducing the content of ethylbenzene, is effected at 454-510 DEG C. and not less than 400 p.s.i.g. in the presence of hydrogen and a catalyst comprising a hydrogenating dehydrogenating component on a support consisting of alumina and 1-15 weight of fluorine which fluorine is added to the support after the hydrogenating / dehydrogenating component. The isomerization of xylenes containing ethylbenzene is effected at 400-1500 p.s.i.g. and 0.1-10 vol.vol./hr. using 100-10,000 ScF/B hydrogen. The catalyst is preferably produced by impregnating alumina with a Group VIA and/or VIII metal or compound thereof and thereafter fluorinating with a compound of the formula XY2F2 in which X is carbon or sulphur and Y is hydrogen or fluorine. | ||||||
| 154 | NL6510791A - | NL6510791 | 1965-08-18 | NL6510791A | 1966-02-28 | |
| 155 | Process for the dealkylation of alkyl aromatic hydrocarbons | GB739062 | 1962-02-26 | GB1007647A | 1965-10-13 | |
| Dealkylation of alkyl aromatic hydrocarbons is carried out by passing the hydrocarbons, together with hydrogen, at an elevated temperature of not more than 520 DEG C. over a catalyst comprising a major proportion of a refractory oxide of Groups II, III or IV, a minor proportion of a platinum group metal and a minor proportion of fluorine, said fluorine being added to the oxide already containing the platinum group metal. Conditions specified are temperatures of 400-520 DEG C., pressures of atmospheric-1500 p.s.i.g., space velocities of 0.1-10 v./v./hr. and hydrogen rate of 1000-15000 S.C.F./B. Catalyst specified is platinum/alumina/fluorine. The dealkylation of a kerosene extract is exemplified. Specification 867,990 is referred to. | ||||||
| 156 | Process for the regeneration of aluminium halide-hydrocarbon sludge | GB2406563 | 1963-06-17 | GB994949A | 1965-06-10 | |
| In hydrocarbon conversion reactions, employing aluminium halide catalyst, aluminium halide catalyst is regenerated from catalyst sludge by hydrogenation in the presence of an antimony halide. Specified reactions are cracking naphthas, kerosenes and gas oils to lower boiling hydrocarbons, polymerizing gaseous olefins to gasoline or lubricating oil, alkylating isoparaffins or aromatic hydrocarbons with olefins, isomerizing paraffins or wax and treating lubricating oil with aluminium chloride. Antimony chloride or bromide is added to give a mixture containing 0.5-99% wt. antimony halide and hydrogenation is effected at 150-250 DEG C. and a hydrogen partial pressure of 14-175 atm. for 5 mins. to 10 hrs. The hydrogen consumption may be 0.32-2.3 mm.3 per kg. of hydrocarbon in the sludge and the hydrogen feed rate up to 10 times the consumption. The hydrogenating gas preferably contains 2-20% vol. of hydrogen halide. The reactor may be heated or a crackable hydrocarbon may be added, the heat of cracking providing the reaction heat. The hydrocarbon may be one boiling in the range 65-550 DEG C. used in an amount referably controlled according to the temperature of 1-8% wt. of the total non-gaseous reaction mixture and is preferably added at at least its incipient cracking temperature. Preferably part or all of the sludge feed is contacted with off-gases from the hydrogenation, e.g. in a stripping-absorption zone positioned above the reaction zone. The reaction zone may be a vertical cylinder having a length to diameter ratio of 10-70:1 through which the superficial gas velocity may be 0.003-0.09 m./sec. The superposed stripping-absorption zone may have a length to diameter ratio of 2-20:1 with 1-10 theoretical stages being suitably packed. Catalyst is recovered from the product mixture by distillation.ALSO:Aluminium halide catalyst is regenerated from catalyst-hydrocarbon sludge by hydrogenation in the presence of antimony halide. Antimony halide is added, if not present in the sludge, to give a mixture containing 0,5-99% wt. antimony halide and the mixture is hydrogenated at 150-250 DEG C. and a hydrogen partial pressure of 14-175 atm. for 5 minutes to 10 hours, the gas preferably containing 2-20% vol. hydrogen halide. The sludge may be stripped before hydrogenation by the hydrogenation off-gases. The hydrogenated product may be used as a catalyst as such or after distillation. | ||||||
| 157 | A process for converting higher boiling hydrocarbons in lower boiling | DEST002396 | 1944-03-14 | DE881496C | 1953-06-29 | FISCHER FRANZ DR; KOCH HERBERT DR; GILFERT WILHELM DR |
| 158 | CATALYST COMBINATION AND PROCESS FOR DIRECT LIQUEFACTION OF CARBONACEOUS MATERIALS BY USING THE SAME | CA2631916 | 2008-05-22 | CA2631916A1 | 2009-01-19 | YAN TAO; SHI HONGXIA; XIAO GANG; HOU XIAOFENG |
| The present invention relates to a catalyst combination and a process for direct liquefaction of carbonaceous materials by using the same, in particular, to a catalyst combination comprising an iodine-containing substance and a sulfur oxide species and a process for direct liquefaction of carbonaceous materials by using the catalyst combination. | ||||||
| 159 | КАТАЛИЗАТОР И СПОСОБ ГИДРОКРЕКИНГА НЕФТЯНОГО СЫРЬЯ С ЕГО ИСПОЛЬЗОВАНИЕМ | RU2003121342 | 2003-07-15 | RU2003121342A | 2005-02-10 | |
| 160 | HYDROCRACKING OF FEEDSTOCKS AND CATALYST THEREFOR | CA2132995 | 1994-09-27 | CA2132995A1 | 1995-03-29 | PRADA RICARDO; GALIASSO ROBERTO; ROMERO YILDA; REYES EDITO; RODRIGUEZ EDILBERTO |
| A tri-elemental catalyst on a support that includes a pentasil crystalline zeolite and is suitable for hydrocracking and hydrogenation of aromaticscontaining petroleum hydrocarbon feedstocks such as hydrotreated cracked feedstock, virgin feedstock, vacuum distillate, middle distillate, mixtures thereof, and the like, is disclosed. The catalyst is suitable for hydrodesulfurization as well as hydrodenitrogenation, thus the feedstock can contain sulfur and nitrogen in addition to the aromatic components. Hydrocracking and aromatics hydrogenation of the petroleum hydrocarbon feedstocks is accomplished under a relatively wide range of process conditions in plural process zones using the tri-elemental catalyst that contains a catalytically active metal phase constituted by a Group VI-B element, a Group VIII first transition series element and a Group VIII second transition series element. In an upstream zone the catalytically active metal phase is supported on a titania-alumina support containing about 5% to about 30% by weight titania in the support. In a downstream zone the catalytically active metal phase is supported on a titania-alumina-pentasil crystalline zeolite support. The preferred pentasil crystalline zeolite is ZSM-5. | ||||||
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