| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 81 | Hydrocarbon conversion process using staggered bypassing of reaction zones | US704224 | 1996-08-23 | US5879537A | 1999-03-09 | Kenneth D. Peters |
| A multistage catalytic hydrocarbon conversion system is disclosed in which hydrocarbons flow serially through at least two reaction zones and through which catalyst particles move. Where three reaction zones are used, the effluent stream from the first reaction zone is split between the second and third reaction zones. One portion of the effluent stream is combined with hydrocarbons that bypassed the first reaction zone, and the combined stream is passed to the second reaction zone. The other portion of the first reaction zone effluent stream and at least a portion of the effluent stream of the second reaction zone are passed to the third reaction zone. This invention is applicable to processes where the first and second reaction zones are susceptible to pinning in that this invention decreases the mass flow through the first and second reaction zones while nevertheless maintaining high hydrocarbon conversion. | ||||||
| 82 | Hydrocarbon upgrading process | US285476 | 1994-08-03 | US5603824A | 1997-02-18 | Chwan P. Kyan; Paul J. Oswald |
| The instant invention discloses a process of upgrading a waxy hydrocarbon feed mixture containing sulfur compounds which boils in the distillate range, in order to reduce sulfur content and 85% point while preserving the high octane of naphtha by-products and maximizing distillate yield. The process employs a single, downflow reactor having at least two catalyst beds and an inter-bed redistributor between the beds. The top bed contains a hydrocracking catalyst, preferably zeolite beta, and the bottom bed contains a dewaxing catalyst, preferably ZSM-5. A desulfurization catalyst may be added to either bed depending on sulfur distribution in the feed. The feed is separated into a lighter, lower boiling stream and a heavier, higher boiling stream. The effluent of the top bed cascades without interbed separation to the inter-bed redistributor, where it is recombined with the lighter stream. The recombined stream then enters the bottom bed for dewaxing. The product comprises a distillate having an increased yield and a naphtha having an increased research octane number, as compared with a feedstock in which the entire stream was hydrocracked. | ||||||
| 83 | Production of low sulfur distillate fuel | US293775 | 1994-08-22 | US5409599A | 1995-04-25 | Mohsen N. Harandi |
| Low sulfur distillate fuel oils such as road diesel oil having a maximum sulfur content of 0.05 weight percent, are produced by segregation of a distillate range feed into a lower boiling fraction and higher boiling fraction with the cut point between the two fractions between about 600.degree. and 650.degree. F. (about 315.degree. to 345.degree. C.). The higher boiling fraction is hydrodesulfurized under relatively severe conditions and then combined with the lower boiling fraction to be hydrodesulfurized under less severe conditions. Operation in this manner enables the refractory dibenzothiophenes to be removed while maintaining a lower hydrogen consumption. | ||||||
| 84 | Distillate fuel production from Fischer-Tropsch wax | US96129 | 1993-07-22 | US5378348A | 1995-01-03 | Stephen M. Davis; Daniel F. Ryan |
| Distillate fuels with excellent cold flow properties are produced from waxy Fischer-Tropsch products by separating the product into a heavier and a lighter fraction, isomerizing the heavier fraction, hydrotreating and isomerizing the lighter fraction, and recovering products in jet and diesel fuel ranges. | ||||||
| 85 | Hydrocarbon conversion process | US46537 | 1993-04-13 | US5364514A | 1994-11-15 | Laura J. Sanborn; Stanley N. Milam; Woodrow K. Shiflett |
| This invention provides an integrated process for converting a hydrocarbon feedstock having components boiling above 300.degree. F. into liquid fuel products boiling in the range of from about 80.degree. F. to about 700.degree. F., which process comprises passing said feedstock to a first stage hydrocracking zone to effect decomposition of organic sulfur and/or nitrogen compounds, passing a portion of the product from said first stage hydrocracking zone to a second stage hydrocracking zone, simultaneously passing the remaining portion of said product from said first stage hydrocracking zone to an aromatics saturation zone, and subsequently passing the product from said hydrocracking zone and said aromatics saturation zone to one or more fractionating zones wherein said products are separated into a tops fraction and a bottoms fraction, with the tops fraction being separated into light gasoline, naphtha, jet fuel and diesel fuel products, and a portion or all of the bottoms fraction being recycled to the hydrocracking zone and/or the aromatics saturation zone following the optional removal of heavies and polynuclear aromatics. | ||||||
| 86 | Integrated process for the production of distillate hydrocarbon | US813522 | 1991-12-26 | US5244565A | 1993-09-14 | Steven P. Lankton; Tom N. Kalnes; Robert B. James, Jr. |
| A process for the production of distillate hydrocarbon from atmospheric fractionation residue and waste lubricants by means of contacting the waste lubricant with a hot hydrogen-rich gaseous stream to increase the temperature of this feed stream to vaporize at least a portion of the distillable hydrocarbonaceous compounds thereby producing a distillable hydrocarbonaceous stream which is immediately hydrogenated in an integrated hydrogenation zone. The vaporization of the waste oil is also conducted in the presence of a vacuum fractionation residue which is produced in the integrated process. The resulting effluent from the integrated hydrogenation zone and a distillable hydrocarbon stream recovered from the atmospheric fraction residue is catalytically converted to produce lower molecular weight hydrocarbon compounds. | ||||||
| 87 | Method of upgrading residua | US694225 | 1991-04-05 | US5203987A | 1993-04-20 | Emiliano de la Fuente |
| Residua comprises upgraded by first partitioning a hydrocracked residua into a vapor fraction and a liquid fraction. The vapor fraction is hydrotreated forming a first hydrotreated product. The liquid fraction is partitioned into a residua fraction and a light liquid fraction. The light liquid fraction can be hydrotreated or hydrocracked to form a hydroprocessed product. The hydrotreated product and the hydroprocessed product are then combined forming a substantially upgraded synthetic crude product refinable as a routine crude in a refinery into products that meet stringent specifications. In particular, residua can be upgraded to make a quality jet fuel fraction and a naphtha fraction containing less than 1 ppmw sulfur and nitrogen. | ||||||
| 88 | Process for hydrotreating olefinic distillate | US198905 | 1988-05-26 | US4864067A | 1989-09-05 | Mohsen N. Harandi; Hartley Owen |
| A process and reactor system is disclosed for hydrotreating a low sulfur containing olefinic distillate and conventional feedstock to a catalytic hydrodesulfurization. The process comprises passing a minor portion of the olefinic distillate to a first hydrotreating zone in admixture with conventional CHD feedstock. A major portion of the olefinic distillate is passed to a second hydrotreating zone in combination with the effluent from the first zone. In this manner the exotherm attributable to olefins hydrogenation is controlled within limits sufficient to avoid very frequent catalyst regeneration. | ||||||
| 89 | Dual catalyst converter and process | US48159274 | 1974-06-21 | US3894937A | 1975-07-15 | BONACCI JOHN C; MITCHELL KENNETH M |
| A catalytic converter and method of operating the same is described for the use of two beds of catalyst of different characteristics arranged in series in the same reactor and provided with valving and operating characteristics such that the two catalysts may be used in the same manner as though they were disposed in parallel reactors.
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| 90 | Process for hydrocracking nitrogen-containing feedstocks | US3657110D | 1970-01-05 | US3657110A | 1972-04-18 | HENGSTEBECK ROBERT J |
| The process comprises introducing a first portion of a feedstock containing at least 20 parts per million of nitrogen into a feedpreparation zone to reduce the nitrogen and sulfur contents thereof; treating the effluent from the feed-preparation zone to separate a hydrogen-containing light gas and a heavy bottoms fraction from the effluent; introducing the treated effluent into a hydrocracking zone; and introducing a second portion of the feedstock containing at least 20 parts per million of nitrogen into the hydrocracking zone at a plurality of points spaced along the length of the hydrocracking zone to provide an increasing amount of nitrogen along the length of the hydrocracking zone in the direction of flow through the hydrocracking zone. The nitrogen-containing feedstock is introduced into the hydrocracking zone at a plurality of points along its length to control effectively the rate of reaction in the hydrocracking zone. The heat of the controlled hydrocracking reaction is used effectively to reduce external heat supplied to the hydrocarbons prior to their entry into the hydrocracking zone.
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| 91 | Process for the production of lubricating oils | US3617482D | 1969-11-10 | US3617482A | 1971-11-02 | EGAN CLARK J |
| Lubricating oil production process comprising hydrocracking in a first zone a hydrocarbon oil feed in the presence of a hydrocracking catalyst comprising silica and alumina and containing more alumina then silica, hydrocracking in a second zone a second hydrocarbon oil feed, together with a waxcontaining hydrocarbon fraction from said first zone, in the presence of a hydrocracking catalyst comprising silica and alumina and containing more alumina than silica, and recovering from the effluent of said second zone at least one light neutral oil having a VI above 100.
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| 92 | Upgrading of coke oven light oils | US3449460D | 1968-06-06 | US3449460A | 1969-06-10 | TARHAN MEHMET ORHAN |
| 93 | Two-stage hydrorefining of asphaltene-containing oils | US3429801D | 1965-12-06 | US3429801A | 1969-02-25 | GLEIM WILLIAM K T; O'HARA MARK J |
| 94 | Black oil conversion and desulfurization process | US59793566 | 1966-11-30 | US3364134A | 1968-01-16 | HAMBLIN ROBERT J J |
| 95 | Multi-stage hydrocracking process | US32594963 | 1963-11-26 | US3243367A | 1966-03-29 | MASON HAROLD F; BRAY BEN G |
| 96 | Rhigh boiling | US3124526D | US3124526A | 1964-03-10 | ||
| 97 | Process for selective hydrogenation of petroleum stocks | US53397855 | 1955-09-13 | US2878179A | 1959-03-17 | HARVEY HENNIG |
| 98 | Desulfurization of crude oils by catalytic high-pressure hydrogenation | US46321354 | 1954-10-19 | US2833697A | 1958-05-06 | WILLI OETTINGER |
| 99 | Production of lubricating oils | US50073255 | 1955-04-12 | US2787582A | 1957-04-02 | WATKINS CHARLES H; DE ROSSET ARMAND J |
| 100 | Combination cocurrent and countercurrent staged hydroprocessing with a vapor stage | US73414 | 1998-05-06 | US6153086A | 2000-11-28 | Ramesh Gupta; Henry Jung; Edward S. Ellis; James J. Schorfheide; Larry L. Iaccino |
| A hydroprocessing process includes a cocurrent flow liquid reaction stage, a countercurrent flow liquid reaction stage and a vapor reaction stage in which feed components are catalytically hydroprocessed by reacting with hydrogen. Both liquid stages both produce a liquid and a vapor effluent, with the cocurrent stage liquid effluent the feed for the countercurrent stage and the countercurrent stage liquid effluent the hydroprocessed product liquid. Both liquid stage vapor effluents are combined and catalytically reacted with hydrogen in a vapor reaction stage, to form a hydroprocessed vapor. This vapor is cooled to condense and recover a portion of the hydroprocessed hydrocarbonaceous vapor components as additional product liquid. The uncondensed vapor is rich in hydrogen and is cleaned up if necessary, to remove contaminants, and then recycled back into the cocurrent stage as hydrogen-containing treat gas. Fresh hydrogen is introduced into the countercurrent stage and the countercurrent stage effluent contains sufficient, and preferably all of the hydrogen for the vapor stage reaction. | ||||||
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