| 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 | Treatment of motor fuel | US63961832 | 1932-10-26 | US2001907A | 1935-05-21 | VLADIMIR IPATIEFF |
| 82 | Process of producing light olefins and aromatics from wide range boiling point naphtha | US17250395 | 2019-06-24 | US11807819B2 | 2023-11-07 | Khalid A. Al-Majnouni; Naif A. Al-Dalaan; Ahmad M. Al-Shehri; Nabil Al-Yasser; Ahmed Al-Zenaidi |
| Systems and methods for processing full range naphtha to produce light olefins are disclosed. The systems and methods include separating the full range naphtha into a light naphtha stream and a heavy naphtha stream and integrating a catalytic cracking with a naphtha reforming to process the light naphtha and heavy naphtha streams. | ||||||
| 83 | Method for the conversion of feedstock containing naphtha to low carbon olefins and aromatics | US17422679 | 2019-01-28 | US11685866B2 | 2023-06-27 | Yinfeng Zhao; Mao Ye; Zhongmin Liu; Hailong Tang; Jing Wang; Jinling Zhang; Tao Zhang; Talal Khaled Al-Shammari |
| Disclosed is a method for producing low carbon olefins and/or aromatics from feedstock comprising naphtha. The method can include the following steps: a) feeding feedstock comprising naphtha into a fast fluidized bed reactor; b) contacting the feedstock with a catalyst under conditions to produce a gas product and spent catalyst; c) separating the gas product to produce a stream comprising primarily one or more low carbon olefins and/or one or more aromatics; d) transporting the spent catalyst to a regenerator; e) regenerating the spent catalyst in the regenerator to form regenerated catalyst; and f) returning the regenerated catalyst to the fast fluidized bed reactor. | ||||||
| 84 | Integrated process for production of gasoline | US16049144 | 2018-07-30 | US10301558B1 | 2019-05-28 | Charles P. Luebke; Lin Jin; Christopher DiGiulio; Mark P. Lapinski |
| An integrated process for production of gasoline has been described. The process includes a C5-C6 isomerization zone, two C7 isomerization zones separate by a deisoheptanizer, and a reforming zone. The use of two C7 isomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The low temperature in first C7 isomerization zone favors the formation of multi-branched C7 paraffins and cyclohexanes and maximizes C5+ yield. The separation between paraffin and cycloalkane in deisoheptanizer becomes easier due to conversion of cycloalkanes to cyclohexanes in the first C7 isomerization zone. Further, the high temperature in second C7 isomerization zone favors the formation of higher octane cyclopentanes over cyclohexanes. An aromatic-containing stream can be introduced to second C7 isomerization zone. The saturation of the aromatics in the second C7 isomerization zone provides heat that increases the reactor outlet temperature in the isomerization reactors to favor cyclopentanes. | ||||||
| 85 | High-toughness materials based on unsaturated polyesters | US14409320 | 2013-06-19 | US10273330B2 | 2019-04-30 | Reinhard Lorenz; Monika Bauer; Sebastian Steffen |
| The present invention relates to unsaturated carboxylic acid ester obtained from or through the use of a source material defined below in formula (I): A(0.9-1.2)(B+C)(1.0) (I) wherein the figures set in parentheses indicate the molar proportion of source material A to the sum of source materials B and C, and wherein the following meanings apply: A: unsaturated dicarboxylic acid, B: a hard diol segment, C: a soft diol segment selected from among compounds having a continuous chain between two hydroxyl groups, which have a length of 5 to 30 atoms, wherein the molar ratio of B:C is between 5:95 and 95:5. Furthermore, it relates to unsaturated polyester resin comprising said unsaturated carboxylic acid ester as defined above and a reactive diluents as well as molded articles, coatings, and surface textiles coated, saturated, laminated, and impregnated from or with a thermoset, which was obtained by hardening said unsaturated polyester resin. | ||||||
| 86 | Methods and apparatuses for an integrated isomerization and platforming process | US15721895 | 2017-09-30 | US10240097B2 | 2019-03-26 | Bryan K. Glover |
| The present disclosure generally relates to methods and systems for reforming and isomerizing hydrocarbons. More particularly, the present disclosure relates to a novel combination of two traditionally separate reforming and isomerization reaction zones. A first hydrocarbon stream comprising C5-C6 hydrocarbons is isomerized in a first isomerization zone. A second hydrocarbon stream comprising C7+ hydrocarbons is reformed thus producing a C7 hydrocarbon stream and a C8 hydrocarbon stream. The reformed C7 stream is then isomerized in a second isomerization zone. | ||||||
| 87 | PROCESS FOR PRODUCING BENZENE FROM A C5-C12 HYDROCARBON MIXTURE | US16130488 | 2018-09-13 | US20190010097A1 | 2019-01-10 | Andrew Davies; Dustin Fickel; Maikel Van Iersel |
| The invention relates to a process for producing benzene, comprising the steps of: (a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h−1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream. | ||||||
| 88 | NON-CATALYTIC HYDROGEN GENERATION PROCESS FOR DELIVERY TO A HYDRODESULFURIZATION UNIT AND A SOLID OXIDE FUEL CELL SYSTEM COMBINATION FOR AUXILIARY POWER UNIT APPLICATION | US16039040 | 2018-07-18 | US20180323458A1 | 2018-11-08 | Thang Viet Pham; Hasan lmran; Mohamed Daoudi |
| A non-catalytic hydrogen generation process is provided that supplies hydrogen to a hydrodesulfurization unit and a solid oxide fuel cell system combination, suitable for auxiliary power unit application. The non-catalytic nature of the process enables use of sulfur containing feedstock for generating hydrogen which is needed to process the sulfur containing feed to specifications suitable for the solid oxide fuel cell. Also, the non-catalytic nature of the process with fast dynamic characteristics is specifically applicable for startup and shutdown purposes that are typically needed for mobile applications. | ||||||
| 89 | Process for producing benzene from a C5-C12 hydrocarbon mixture | US15318136 | 2015-06-01 | US10118874B2 | 2018-11-06 | Andrew Davies; Dustin Fickel; Maikel Van Iersel |
| The invention relates to a process for producing benzene, comprising the steps of: (a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 A and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h−1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream process for producing benzene from a c5-c12 hydrocarbon mixture | ||||||
| 90 | Power generation using independent dual organic Rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and continuous-catalytic-cracking-aromatics facilities | US15087440 | 2016-03-31 | US09803507B2 | 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 organic Rankine cycle (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. | ||||||
| 91 | Gasoline upgrading process | US104691 | 1993-08-11 | US5397455A | 1995-03-14 | Hye K. C. Timken |
| Low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by treatment over an acidic catalyst, preferably an intermediate pore size zeolite such as ZSM-5 with controlled diffusion characteristics. The treatment over the acidic catalyst in the second step restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha. In favorable cases, using feeds of extended end point such as heavy naphthas with 95 percent points above about 380.degree. F. (about 193.degree. C.), improvements in both product octane and yield relative to the feed may be obtained. | ||||||
| 92 | Benzene upgrading reformer integration | US375172 | 1989-07-03 | US4950823A | 1990-08-21 | Mohsen N. Harandi; Hartley Owen |
| A process and apparatus are disclosed for the production of gasoline from a C.sub.4.sup.- fuel gas containing ethene and propene and catalytic reformate containing C.sub.6 to C.sub.8 aromatics. The C.sub.4.sup.- fuel gas is contacted with debutanized catalytic reformate over a zeolite catalyst under process conditions to convert ethene and propene in the C.sub.4.sup.- fuel gas to C.sub.5.sup.+ aliphatic and aromatic hydrocarbon gasoline and to convert C.sub.6 to C.sub.8 aromatics in the reformate to C.sub.7 to C.sub.11 aromatic hydrocarbon gasoline. Reformer fractionation system containing debutanizer column and separator stabilizes effluent gasoline and recycles unconverted light aromatics. | ||||||
| 93 | Conversion of alkycyclopentanes to aromatics | US420541 | 1982-09-20 | US4434311A | 1984-02-28 | Waldeen C. Buss; Thomas R. Hughes |
| A method is disclosed for the dehydroisomerization of alkylcyclopentanes using a catalyst comprising a large-pore zeolite, a Group VIII metal, and an alkaline earth metal. | ||||||
| 94 | Process for producing gas from oil | US63449845 | 1945-12-12 | US2561419A | 1951-07-24 | HENRY SCHUTTE AUGUST |
| 95 | Gasoline manufacture | US42865642 | 1942-01-29 | US2460303A | 1949-02-01 | MCALLISTER SUMNER H; JOHN ANDERSON; PETERSON WALTER H |
| 96 | POWER GENERATION FROM WASTE HEAT IN INTEGRATED AROMATICS AND NAPHTHA BLOCK FACILITIES | PCT/US2016/048210 | 2016-08-23 | WO2017035149A1 | 2017-03-02 | NOURELDIN, Mahmoud Bahy Mahmoud; AL SAED, Hani Mohammed; BUNAIYAN, Ahmad Saleh |
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. |
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| 97 | RECOVERY AND RE-USE OF WASTE ENERGY IN INDUSTRIAL FACILITIES | PCT/US2016/048078 | 2016-08-22 | WO2017035093A1 | 2017-03-02 | NOURELDIN, Mahmoud Bahy Mahmoud; AL SAED, Hani Mohammed; BUNAIYAN, Ahmad Saleh; KAMEL, Akram Hamed Mohamed |
Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described. |
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| 98 | RECOVERY AND RE-USE OF WASTE ENERGY IN INDUSTRIAL FACILITIES | PCT/US2016/048067 | 2016-08-22 | WO2017035084A1 | 2017-03-02 | NOURELDIN, Mahmoud Bahy Mahmoud; AL SAED, Hani Mohammed; BUNAIYAN, Ahmad Saleh; KAMEL, Akram Hamed Mohamed |
Configurations and related processing schemes of direct or indirect (or both) intra-plants and thermally coupled heating systems synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of direct or indirect (or both) intra-plants and thermally coupled heating systems synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described. |
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| 99 | RECOVERY AND RE-USE OF WASTE ENERGY IN INDUSTRIAL FACILITIES | PCT/US2016/048042 | 2016-08-22 | WO2017035075A1 | 2017-03-02 | NOURELDIN, Mahmoud Bahy Mahmoud; AL SAED, Hani Mohammed; BUNAIYAN, Ahmad Saleh; KAMEL, Akram Hamed Mohamed |
Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter- plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter- plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described. |
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| 100 | INTEGRATED PROCESSES AND SYSTEMS FOR REFORMING AND ISOMERIZING HYDROCARBONS | PCT/US2015/064180 | 2015-12-07 | WO2016094264A3 | 2016-06-16 | EIZENGA, Donald A.; SHECTERLE, David James; KAYE, Joel; VAN ZILE, Charles Paul; ZHU, Xin X.; LONG, Ronald Joseph |
Processes and systems are provided for reforming and isomerizing hydrocarbons to produce octane upgraded hydrocarbons. The process involves providing a reforming feedstream to a reforming zone containing a reforming catalyst and operating the reforming zone at reforming conditions including reforming pressure in a range of from 1 to 18 atmospheres to generate a reforming zone effluent. The reforming zone effluent is separated to form a net gas stream comprising primarily hydrogen and a liquid reforming product stream, and then providing the net gas stream and an isomerization feedstream to an isomerization zone containing an isomerization catalyst. The isomerization zone is operated at an isomerization pressure that is greater than the reforming pressure, to produce an isomerization zone effluent. The system for reforming and isomerizing hydrocarbons includes a reforming zone containing a reforming catalyst, a reforming separator, an isomerization zone containing an isomerization catalyst, and an isomerization separator. |
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