| 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 | PROCESS AND APPARATUS FOR PRODUCING GASOLINE | US12176290 | 2008-07-18 | US20100012552A1 | 2010-01-21 | Robert B. James, JR.; Deng-Yang Jan; Robert J. Schmidt |
| One exemplary embodiment can be a process for producing a gasoline. The process can include contacting a feed having a naphtha and recycling at least a portion of the reaction zone effluent to the one or more reforming reaction zones. Generally, the reformate includes no more than about 15%, by volume, benzene, with a UZM-8 catalyst in one or more reforming reaction zones to produce a reaction zone effluent. | ||||||
| 82 | Process for catalytically reforming a hydrocarbonaceous feedstock | US10508159 | 2003-03-20 | US20050139516A1 | 2005-06-30 | Martin Nieskens; Gerrit Den Otter |
| A process for catalytically reforming a gasoline boiling range hydrocarbonaceous feedstock in the presence of hydrogen involving the following steps: (a) reforming at least 5 vol % and at most 50 vol % of the feedstock in a first reforming unit having a fixed bed of catalyst particles; (b) passing the effluent stream of the first reforming unit to a separation zone having a separator and a stabilizer to produce a hydrogen-rich gaseous stream, a C4− hydrocarbon stream and a first reformate; (c) reforming the remainder of the feedstock and at least part of the first reformate in a second reforming unit having one or more serially connected reaction zones, each having a moving catalyst bed, which are operated in a continuously catalyst regeneration mode; and, (d) passing the effluent stream of the second reforming unit to a separation zone having a separator and a stabilizer to produce a hydrogen-rich gaseous stream, a C4− hydrocarbon stream and a second reformate. | ||||||
| 83 | 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. | ||||||
| 84 | Isomerization and adsorption process with benzene saturation | US109558 | 1993-08-20 | US5453552A | 1995-09-26 | Lynn H. Rice; Robert S. Haizmann; Mark S. Turowicz |
| An advantageous integration of benzene saturation for a light paraffin containing feedstock in a light paraffin isomerization and adsorption system maintains isomerization conversion while reducing benzene levels. The process improves the efficiency of the isomerization and saturation zones by saturating benzene from a light paraffin containing stream and adsorbing normal hydrocarbons from the saturation zone effluent stream together with normal hydrocarbons from an isomerization zone effluent. The isomerization zone effluent comprises converted hydrocarbons from a light paraffin containing feedstream having a relatively low benzene concentration. Saturating the high benzene feed in a first step of saturation and passing the low benzene containing feedstream through the isomerization zone independent of the benzene saturation removes normal hydrocarbons from the isomerization step to improve equilibrium and provides a gaseous phase for desorption and a heavier hydrocarbon phase for adsorption to improve product recovery and normal paraffin recovery. | ||||||
| 85 | Integrated reforming and alkylation process for low benzene reformate | US960339 | 1992-10-13 | US5273644A | 1993-12-28 | David A. Wegerer |
| The invention is a lower cost combined reforming-benzene alkylation process. The unstabilized liquid product recovered from the reforming reaction zone is not stabilized by passage into a stripping column for the removal of C.sub.4 -minus hydrocarbons but is instead split into light and heavy fractions, with the light, benzene-containing fraction being passed directly into an alkylation zone. | ||||||
| 86 | Reformulated-gasoline production | US796101 | 1991-11-21 | US5198097A | 1993-03-30 | Paula L. Bogdan; R. Joe Lawson; J. W. Adriaan Sachtler |
| A process combination is disclosed to reduce the aromatics content and increase the oxygen content of a key component of gasoline blends. A naphtha feedstock having a boiling range usually suitable as catalytic-reforming feed is processed by selective isoparaffin synthesis to yield lower-molecular weight hydrocarbons including a high yield of isobutane. A portion of the isobutane is processed to yield an ether component by dehydrogenation to yield isobutene followed by etherification. Part of the isobutane and isobutene are alkylated to produce an alkylate component. The synthesis light naphtha may be upgraded by isomerization. The heavier portion of the synthesis naphtha is processed in a reformer. A gasoline component containing oxygen as ether and having a reduced aromatics content and increased volumetric yield relative to reformate of the same octane number is blended from the net products of the above processing steps. | ||||||
| 87 | 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.
|
||||||
| 88 | Catalytic reforming process | US3516924D | 1968-04-19 | US3516924A | 1970-06-23 | FORBES JAMES T |
| 89 | Production of high octane paraffinic gasolines | US46504842 | 1942-11-09 | US2373674A | 1945-04-17 | CRAWFORD CHESTER C; FULLER DONALD L; GREENSFELDER BERNARD S |
| 90 | Treatment of hydrocarbons | US30975639 | 1939-12-18 | US2314435A | 1943-03-23 | ALLENDER SAMUEL S |
| 91 | Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis | US17948718 | 2022-09-20 | US20230046694A1 | 2023-02-16 | Vincent D. McGahee; Daniel M. Hasenberg |
| A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different. | ||||||
| 92 | Methods and systems for optimizing mechanical vapor compression and/or thermal vapor compression within multiple-stage processes | US17374962 | 2021-07-13 | US11364449B2 | 2022-06-21 | Lynn Allen Crawford; William Bryan Schafer, III |
| The present invention utilizes mechanical vapor compression and/or thermal vapor compression integrating compression loops across multiple process stages. A sequential network of compressors is utilized to increase the pressure and condensing temperature of the vapors within each process stage, as intra-vapor flow, and branching between process stages, as inter-vapor flow. Because the vapors available are shared among and between compressor stages, the number of compressors can be reduced, improving economics. Balancing vapor mass flow through incremental compressor stages which traverse multiple process stages by splitting vapors between compressor stages enables the overall vapor-compression system to be tailored to individual process energy requirements and to accommodate dynamic fluctuations in process conditions. | ||||||
| 93 | Methods and systems for electrifying, decarbonizing, and reducing energy demand and process carbon intensity in industrial processes via integrated vapor compression | US17374959 | 2021-07-13 | US11291927B2 | 2022-04-05 | Lynn Allen Crawford; William Bryan Schafer, III |
| This disclosure provides systems and methods that utilize integrated mechanical vapor or thermal vapor compression to upgrade process vapors and condense them to recover the heat of condensation across multiple processes, wherein the total process energy is reduced. Existing processes that are unable to recover the heat of condensation in vapors are integrated with mechanical or thermal compressors that raise vapor pressures and temperatures sufficient to permit reuse. Integrating multiple processes permits vapor upgrading that can selectively optimize energy efficiency, environmental sustainability, process economics, or a prioritized blend of such goals. Mechanical or thermal vapor compression also alters the type of energy required in industrial processes, favoring electro-mechanical energy which can be supplied from low-carbon, renewable sources rather than combustion of carbonaceous fuels. | ||||||
| 94 | Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis | US16860638 | 2020-04-28 | US11149211B2 | 2021-10-19 | Vincent D. McGahee; Daniel M. Hasenberg |
| A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different. | ||||||
| 95 | Power generation from waste energy in industrial facilities | US15718687 | 2017-09-28 | US10961873B2 | 2021-03-30 | Mahmoud Bahy Mahmoud Noureldin; Hani Mohammed Al Saed; Ahmad Saleh Bunaiyan |
| Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified. | ||||||
| 96 | Paraxylene production from naphtha feed | US16454839 | 2019-06-27 | US10941356B2 | 2021-03-09 | Yufeng He; Qi Xu |
| Increased paraxylene production through the use of a split feed reforming process, wherein hydrotreated naphtha is split into light, middle and heavy fractions. Each fraction is reformed separately to generate streams containing aromatic compounds. These streams can further be processed and can undergo dealkylation, transalkylation, disproportionation, isomerization, and separation steps to maximize paraxylene production. In addition, some streams are recycled or recombined in order to maximize paraxylene production. | ||||||
| 97 | Fuel composition for GCI engines and method of production | US15872796 | 2018-01-16 | US10260015B2 | 2019-04-16 | Christopher D. Gosling; Mary Jo Wier; Gautam T. Kalghatgi |
| GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26° C. to about 38° C. and a final boiling point in a range of about 193° C. to less than 250° C., a density of about 0.72 kg/l to about 0.8 kg/l at 15° C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream. | ||||||
| 98 | POWER GENERATION FROM WASTE ENERGY IN INDUSTRIAL FACILITIES | US15718687 | 2017-09-28 | US20180016946A1 | 2018-01-18 | Mahmoud Bahy Mahmoud Noureldin; Hani Mohammed Al Saed; Ahmad Saleh Bunaiyan |
| Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified. | ||||||
| 99 | Power generation using independent dual organic rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and atmospheric distillation-naphtha hydrotreating-aromatics facilities | US15087518 | 2016-03-31 | US09803511B2 | 2017-10-31 | Mahmoud Bahy Mahmoud Noureldin; Hani Mohammed Al Saed; Ahmad Saleh Bunaiyan |
| Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified. | ||||||
| 100 | Catalytic reforming process with dual reforming zones and split feed | US13924925 | 2013-06-24 | US09206362B2 | 2015-12-08 | Robert S. Haizmann; Bryan K. Glover |
| A process for the conversion of paraffins and olefins in a hydrocarbon feedstream to aromatics is presented. The process includes separating the hydrocarbon feedstream into two separate streams, a lighter hydrocarbon stream and a heavier hydrocarbon stream, and processing each of the streams separately. The process includes passing the light stream through a series of reforming units and adding the heavy stream at a downstream position to pass through a subsequent reforming unit. | ||||||
QQ群二维码
意见反馈
意见反馈