| 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 | JPH06504072A - | JP51710391 | 1991-10-30 | JPH06504072A | 1994-05-12 | |
| 142 | Catalytic hydrogenation of heavy hydrocarbon oil | JP26187191 | 1991-10-09 | JPH0598270A | 1993-04-20 | YOSHIDA MITSURU; II KENICHI; KASHIMA KAZUHIRO |
| PURPOSE:To provide the title process by which a naphtha fraction and a kerosene and gas oil fraction can be efficiently produced from a heavy hydrocarbon oil in high yields. CONSTITUTION:The title process comprises hydrodemetallizing a heavy hydrocarbon oil, hydrocracking the product, and hydrodesulfurizing and hydrodenitrogenating the hydrocracking product. | ||||||
| 143 | Refining of heavy slurry oil fraction | JP5690591 | 1991-03-20 | JPH04227792A | 1992-08-17 | POORU ARAN EEGAATAA JIYUNIA; JIERARUDO ARAN HOUERU; EDOWAADO ROORENSU SUGURIYUU ZA; KERII JIYOOJI NOTSUPU |
| PURPOSE: To refine a heavy slurry oil fraction at good efficiency by dispersing catalyst fines in a feed oil, passing the mixture through a hydrovisbreaker to lower the viscosity, separating the effluent into higher and lower boiling fractions and passing the respective fractions into a cracking unit so as to convert them into lower-molecular-weight oil products. CONSTITUTION: In a process for converting an oil containing heavy hydrocarbons, a feed stock containing cracking catalyst fines is passed through a hydrovisbreaker 24 to lower the viscosity of the feed oil, the hydrovisbreaker effluent is separated into at least one low-boiling fraction and a high-boiling fraction in a separator 30 to incorporate the high-boiling fraction in the dispersed cracking catalyst fines. Next, the at least one low-boiling fraction is discharged as a product stream from the separator 30 and passed to a cracking unit 36 to convert it into lower molecular weight hydrocarbon product oil, and the higher boiling fraction containing the dispersed cracking catalyst fines is passed into a catalytic cracking unit 44 to convert the higher boiling fraction into lower molecular weight hydrocarbon products. Thus, a heavy slurry oil fraction is refined by cracking. COPYRIGHT: (C)1992,JPO | ||||||
| 144 | Preparation of low-sulfur and high-sulfur cokes | JP32853189 | 1989-12-20 | JPH03199290A | 1991-08-30 | BURUUSU EE NIYUUMAN; BARATSUTO ESU CHIYAHAA |
| PURPOSE: To provide a process for preparing low-sulfur and high-sulfur cokes which can efficiently obtain low-sulfur and low-sulfur cokes respectively from a heavy fraction and a light fraction by catalytically hydrogenating an untreated heavy fuel oil to lower the sulfur content, separating the product into a heavy fraction and a light fraction, subjecting each fraction to delay coking, and then conducting baking. CONSTITUTION: In preparing a low-sulfur coke and a high-sulfur coke from a single starting material, an untreated heavy fuel oil 2, such as a still residue oil, is catalytically hydrogenated with hydrogen 6 in a hydrogenator 4 to lower the sulfur content of the product to not more than 0.75 wt.%, the hydrogenation product is separated by means of a fractionator 10 into a heavy fraction 42 and a light fraction 14, the light fraction and the heavy fraction are subjected to delay coking respectively in coke ovens 16, 44, and the resultant crude coke products are baked respectively in baking machines 24, 52. Thus, a low-sulfur baked coke 26 is obtd. from a coked light fraction, while a high-sulfur baked coke 54 is obtd. from a coked heavy fraction. COPYRIGHT: (C)1991,JPO | ||||||
| 145 | Method of converting hydrocarbon | JP7231476 | 1976-06-21 | JPS523604A | 1977-01-12 | YAKOBU UAN KURINKEN; PEETERU RADEYURU |
| 146 | JPS4866104A - | JP12174472 | 1972-12-06 | JPS4866104A | 1973-09-11 | |
| 147 | Integrated staged catalytic cracking and hydroprocessing process (JHT-9614) | US702347 | 1996-08-23 | US5770044A | 1998-06-23 | Edward S. Ellis; Ramesh Gupta; Martin G. Bienstock |
| Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step. | ||||||
| 148 | Process for converting olefinic hydrocarbons using spent FCC catalyst | US674963 | 1996-07-03 | US5702589A | 1997-12-30 | Chih-Hao Mark Tsang; Randall Hughes Petty; Glenn Allen Clausen; Charles Henry Schrader |
| Disclosed is a process for converting olefinic hydrocarbons using spent FCC catalysts which comprises using spent FCC catalysts, optionally containing spent FCC additives, in the reactor/stripper part of the FCCU, instead of or in addition to a separate olefin upgrader, to upgrade C.sub.2 -C.sub.8 oligomerizable olefins, preferably propylene and ethylene, into C.sub.4 /C.sub.5 olefins and isoparaffins as well as gasoline, wherein feedstock can be product streams of the FCCU containing propylene/ethylene such as, for example, the absorber and depropanizer overheads. | ||||||
| 149 | Integrated staged catalytic cracking and hydroprocessing process | US292625 | 1994-08-17 | US5582711A | 1996-12-10 | Edward S. Ellis; Ramesh Gupta; Martin G. Bienstock |
| Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step. | ||||||
| 150 | Process for converting heavy hydrocarbon oil into light hydrocarbon fuel | US81981 | 1993-06-23 | US5395511A | 1995-03-07 | Junichi Kubo; Tadakazu Yamashita; Osamu Kato |
| A process is provided for converting a heavy hydrocarbon oil into light hydrocarbon fuels by thermal cracking or hydrocracking, which comprises adding to about 100 parts by weight of the heavy hydrocarbon oil feedstock (A) about 0.1 to 50 parts by weight of a substance (B) which is a hydrogenated oil obtained by aromatic ring hydrogenation of about 430.degree.-600.degree. C. thermal-treated or cracked petroleum feedstock product oil boiling higher than about 200.degree. C. to hydrogenate abot 20 to 90% of the aromatic rings present. | ||||||
| 151 | Refining of heavy slurry oil fractions | US516863 | 1990-04-30 | US5080777A | 1992-01-14 | Paul A. Aegerter, Jr.; Jerald A. Howell; Edward L. Sughrue, II; Kelly G. Knopp |
| For upgrading heavy slurry oil containing catalyst fines from a catalytic cracking operation, the viscosity of the slurry oil is lowered in a hydrovisbreaking process step. In a preferred embodiment an admixture of the fines containing slurry oil and a metal containing resid oil fraction, resulting from a crude distillation, is passed through the hydrovisbreaker. The hydrovisbreaker effluent is separated into higher and lower boiling fractions with the lower boiling fraction preferably passed through a cracking unit so as to covert the lower boiling fraction to lower molecular weight hydrocarbon products. | ||||||
| 152 | Combination process for the conversion of a residual asphaltene-containing hydrocarbonaceous stream to maximize middle distillate production | US916754 | 1986-10-08 | US4721557A | 1988-01-26 | Darrell W. Staggs |
| A process for the conversion of residual asphaltene-containing hydrocarbonaceous charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption. | ||||||
| 153 | Catalytic hydroconversion of residual stocks | US148077 | 1980-05-12 | US4302323A | 1981-11-24 | Nai Y. Chen |
| Hydrotreating and hydrocracking of heavy residual stocks are improved with respect to conversion, product distribution, product quality and system operability by mixing with the heavy charge a substantial proportion of an aromatic light distillate oil (light gas oil) of high nitrogen content. | ||||||
| 154 | Hydrodenitrogenation of shale oil using two catalysts in parallel reactors | US643190 | 1975-12-22 | US4022683A | 1977-05-10 | Joseph A. Bludis; David Lyzinski; Joel D. McKinney; Raynor T. Sebulsky; Harry C. Stauffer |
| A process for hydrodenitrogenation of shale oil comprising fractionating the shale oil into relatively light and heavy fractions, passing the relatively light fraction through a zone containing a catalyst comprising supported molybdenum and Group VIII metal and passing the relatively heavy fraction through a zone containing a catalyst comprising supported tungsten and Group VIII metal. | ||||||
| 155 | Process for making synthetic fuel gas from crude oil | US35979173 | 1973-05-14 | US3929430A | 1975-12-30 | DIXON ROLLAND E |
| A synthetic fuel gas is produced from crude oil by a combination of inter-related steps which separate the oil into several fractions, a first ethane and lighter gaseous fraction, a further gas fraction containing propane and butane, a gasoline containing fraction boiling up to, about 400* F, and a heavy oil or residual fraction, the first two fractions are treated with caustic to remove sulfur and sulfur compounds therefrom, the third fraction is hydrodesulfurized and the fourth fraction is catalytically cracked to extinction to produce gaseous products and an additional gasoline fraction which is hydrodesulfurized whereupon all except the first fraction are combined and then converted by known operation to produce a synthetic natural gas or fuel. This gas or fuel can be combined with the first gas fraction either before or after hydrogen has been removed from it.
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| 156 | Upgrading crude oil by combination processing | US49742874 | 1974-08-14 | US3928175A | 1975-12-23 | OWEN HARTLEY |
| The combination processing concept described involves using a low severity reforming operation primarily as a source of hydrogen for CHD processing and other treating operations in the production of low octane reformate (90-95 R+O) which is then upgraded by cracking over a crystalline aluminosilicate catalyst to produce a higher octane gasoline boiling product. Alkylation of reformer and FCC light ends contributes to gasoline boiling product yields.
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| 157 | Manufacture of methane-containing gases using an integrated fluid coking and gasification process | US40756673 | 1973-10-18 | US3901667A | 1975-08-26 | HERRMANN JOHN W |
| A petroleum refinery process for converting sulfur-containing crude oil into a methane-containing gas and low sulfur oil, wherein the gaseous effluent of an integrated fluid coking and coke gasification process is desulfurized and utilized as incremental feed for the methanation stage of a naphtha gasification process.
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| 158 | Integrated process combining hydrofining and steam cracking | US31731372 | 1972-12-21 | US3855113A | 1974-12-17 | GOULD G |
| An integrated process for hydroconverting and steam cracking hydrocarbons is disclosed, comprising hydroconverting (particularly hydrodesulfurizing) a hydrocarbon to produce a hydroconverted hydrocarbon and heat; generating steam, using as part of the energy required the heat produced in the hydroconversion step; and contacting the hydroconverted hydrocarbon and the steam in a steam-cracking zone to form lowsulfur-content products. Alternatively, or in conjunction with the heat from the hydroconversion step, the heat produced in hydroconverting a lighter hydrocarbon fraction can be used in producing the steam.
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| 159 | Integrated process combining catalytic cracking with hydrotreating | US3801495D | 1972-05-19 | US3801495A | 1974-04-02 | GOULD G |
| AN INTEGRATED PROCESS IS DISCLOSED, COMPRISING CATALYTICALLY CRACKING A HYDROCARBON FEEDSTOCK IN A CATALYTIC CRACKING ZONE; PASSING THE GAS OIL PORTION OF THE EFFLUENT FROM THE CATALYTIC CRACKING ZONE TO A HYDROTREATING ZONE; REGENERATING THE CATALYTIC CRACKING CATALYST USED IN THE CATALYTIC CRACKING ZONE BY BURNING CARBONACEOUS DEPOSITS THEREFROM, THEREBY PRODUCING HEAT; HEATING WATER TO PRODUCE STEAM USING THIS HEAT; PRODUCING HYDROGEN FROM THIS STEAM; PASSING AT LEAST A PORTION OF THE HYDROGEN FORMED TO THE HYDROTREATING ZONE; AND CATALYTICALLY HYDROTREATING THE GAS OIL PORTION IN THE HYDROTREATING ZONE. ALTERNATIVELY, THE HYDROGEN CAN BE PRODUCED BY REACTING THE CARBONACEOUS DEPOSITS ON THE CATALYTIC CRACKING CATALYST WITH STEAM.
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| 160 | Igh octane gasoline combination cracking process for converting paraffinic naphtha into h | US3758628D | 1971-12-20 | US3758628A | 1973-09-11 | STRICKLAND J; BUNN D |
| A process for manufacturing high octane gasoline from a low octane paraffinic naphtha, which comprises hydrocracking a first portion of the naphtha to yield a C4 fraction comprising isobutane and a hydrocracked light naphtha fraction having a relatively high octane number, catalytically cracking a second portion of the naphtha to yield a C3-C4 fraction comprising propylene, butylenes and isobutane and a catalytically cracked light naphtha fraction having a relatively high octane number, and reacting, in an alkylation zone the hydrocracked C4 fraction and the catalytically cracked C3-C4 fraction to yield a high octane gasoline alkylate. The proportion of naphtha charged to the hydrocracking zone and the catalytic cracking zone are adjusted such that isobutane, butylene and propylene charge to the alkylation zone are in stoichiometric balance.
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