| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 61 | ディーゼル水素処理・水素化分解及び大気圧蒸留分解ナフサ水素処理・芳香族化合物施設における廃熱システムから独立した2個の有機ランキンサイクルを用いた発電 | JP2018510765 | 2016-08-23 | JP6816117B2 | 2021-01-20 | ヌレディン,マフムード バイ マフムード; アル サード,ハニ ムハンマド; ベナン,アーメド サレ |
| 62 | Manufacturing methods and gasoline composition of the gasoline base material | JP2006040710 | 2006-02-17 | JP4851198B2 | 2012-01-11 | 康宏 戸井田; 康一 松下 |
| 63 | Catalytic reforming process of hydrocarbon feedstock | JP2003576544 | 2003-03-20 | JP4260025B2 | 2009-04-30 | オッテア ゲリッツ・ジャン・デン; マルティン・ジェン・ピエーレ・コーネリズ・ニエスケンズ |
| 64 | A method of using a zig-zag bypass the reaction zone for processing capacity improvement | JP5887999 | 1999-03-05 | JP4018835B2 | 2007-12-05 | ディ．ピータース ケネス |
| 65 | Process for the conversion hydrocarbon | JP2000504083 | 1998-06-01 | JP2001510857A | 2001-08-07 | セカンド サフリュー、エドワード、ローレンス、ザ; ドレイク、チャールズ、アルフレッド; ラブ、スコット、ダグラス |
| (57)【要約】 炭化水素の転化方法が、１）反応器（１０）で炭化水素供給材料、例えばガソリンを、炭化水素の転化に有効な条件下で触媒に接触させて、炭化水素を芳香族炭化水素とオレフィンを含む製品流に転化し；２）装置（２０）で製品流を、分子当たり６個以下の炭素原子をもつ炭化水素を主に含む軽質留分、Ｃ 6 −Ｃ 8芳香族炭化水素と非芳香族炭化水素を含む中間留分、と芳香族化合物を含み、装置（３０）中のＣ 9 ＋留分に分け；３）中間留分からＣ 6 −Ｃ 8芳香族炭化水素を分離し；４）装置（５０）で軽質留分から分子当たり５個またはそれ以上の炭素原子をもつ炭化水素（Ｃ 5 ＋炭化水素）を分離する；工程から構成されている。 | ||||||
| 66 | JPS5726631B2 - | JP10426677 | 1977-09-01 | JPS5726631B2 | 1982-06-05 | |
| 67 | 벤젠 및 톨루엔의 제조를 향상시키기 위한 방법 | KR1020207015280 | 2018-11-16 | KR1020200092969A | 2020-08-04 | |
| 68 | C8 방향족 혼합물의 분리 방법 | KR1019950020856 | 1995-07-14 | KR1019970006464A | 1997-02-21 | 박상훈; 이상일; 최선; 황두범; 오승훈; 김용승; 최준태; 서현주; 박남수; 배재영; 이인우 |
| 본 발명은 C 8 방향족 혼합물을 분리 및 이성화반응시켜 파라크실렌, 올소크실렌, 벤젠을 제조하며, 원료인 C 8 방향족 혼합물은 전량 크실렌분리탑으로 주입하는 공정에 있어서, 원료중 일부 또는 전부를 이성화대역으로 일차 주입시키므로써 파라크실렌 및 올소크실렌의 생산량을 증가시키는 C 8 방향족 혼합물의 분리방법에 관한 것이다. | ||||||
| 69 | 씨 4 유분의 중합에 의한 프레미엄 가솔린의 제조 과정 | KR1019840003545 | 1984-06-22 | KR1019850000364A | 1985-02-26 | 베르나르쥐겡; 쟝미껠 |
| 내용없음. | ||||||
| 70 | PROCESS FOR CONVERTING OLEFINS TO DISTILLATE FUELS | US17872714 | 2022-07-25 | US20240025821A1 | 2024-01-25 | Ashish Mathur; Charles Luebke; Manuela Serban; Den-Yang Jan; Eseoghene Jeroro; Hosoo Lim |
| A process for dimerizing and oligomerizing olefins to distillate fuels which manages the dimerization exotherm by diluting it with paraffins which are inert in the dimerization. The olefin stream can also be split and fed to multiple dimerization reactors to further reduce the heat generated. The ethylene feed can also be cooled before entering the dimerization reactor. The paraffins can be obtained from saturating oligomerized effluent. | ||||||
| 71 | 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. | ||||||
| 72 | Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis | US17398594 | 2021-08-10 | US11492558B2 | 2022-11-08 | 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. | ||||||
| 73 | Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis | US16745787 | 2020-01-17 | US11103843B2 | 2021-08-31 | 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. | ||||||
| 74 | PROCESSES FOR CONVERTING C2-C5 HYDROCARBONS TO GASOLINE AND DIESEL FUEL BLENDSTOCKS | US16918324 | 2020-07-01 | US20200331824A1 | 2020-10-22 | Chris D'Acosta; Jeffery Miller; Robert Hoch |
| Disclosed herein are processes for the production of hydrocarbon fuel products from C2-5 alkanes. Methane is converted to ethylene in a methane thermal olefination reactor operating at a temperature of at least 900° C. and a pressure of at least 150 psig, and without a dehydrogenation catalyst or steam. C2-5 alkanes are converted to olefins in a C2-5 thermal olefination reactor operating at a temperature, pressure and space velocity to convert at least 80% of the alkanes to C2-5 olefins. The ethylene and C2-5 olefins are passed through an oligomerization reactor containing a zeolite catalyst and operating at a temperature, pressure and space velocity to crack, oligomerize and cyclize the olefins. In one aspect, methane in the effluent of the oligomerization reactor is recycled through the C2-5 thermal olefination reactor. Methods for the thermal olefination of methane are also disclosed. | ||||||
| 75 | Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis | US15862266 | 2018-01-04 | US10633603B2 | 2020-04-28 | 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. | ||||||
| 76 | Reformate process for producing a fuel from biomass | US15239690 | 2016-08-17 | US10196570B2 | 2019-02-05 | Jeffrey C. Trewella |
| Naphtha compositions with enhanced reformability are provided. The naphtha compositions can be derived from biomass, can exhibit improved N+2A values, and can be used as a reformer feedstock with little or no processing. | ||||||
| 77 | 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. | ||||||
| 78 | Initial hydrotreating of naphthenes with subsequent high temperature reforming | US13327212 | 2011-12-15 | US09024098B2 | 2015-05-05 | Mark D. Moser; David A. Wegerer; Manuela Serban; Kurt M. VandenBussche |
| A process for the production of aromatics through the reforming of a hydrocarbon stream is presented. The process utilizes the differences in properties of components within the hydrocarbon stream to increase the energy efficiency. The differences in the reactions of different hydrocarbon components in the conversion to aromatics allows for different treatments of the different components to reduce the energy used in reforming process. | ||||||
| 79 | Process for reforming hydrocarbon cuts | US13281582 | 2011-10-26 | US09023194B2 | 2015-05-05 | Eric Sanchez; Jacques Rault; Pierre Yves Le Goff; Christophe Pierre; Joana Fernandes |
| A process for reforming a feed composed of one or more hydrocarbon cuts containing 9 to 22 carbon atoms which includes, at least one first step for reforming the feed in at least one reforming unit, during which a stream of hydrogen is produced and at least one first step for distillation of the effluent from the reforming unit in the presence of a reforming catalyst in order to obtain 4 cuts. The 4 cuts are, a liquefied petroleum gas cut (LPG) (A), a C5-C8 cut: naphtha (B), a C9-C15 cut: densified kerosene (C), and a C16-C22 cut: densified gas oil cut (D). The invention also concerns the device for carrying out this process. | ||||||
| 80 | Process for increasing aromatics production | US13856349 | 2013-04-03 | US08926830B2 | 2015-01-06 | Gregory J. Gajda; Mary J. Wier; Clayton Colin Sadler |
| Processes for producing aromatics from a naphtha feedstream are provided. An exemplary process includes passing the feedstream to a fractionation unit, thereby generating a first stream including hydrocarbons having less than 8 carbon atoms and a second stream including hydrocarbons having at least 8 carbon atoms. The first stream is passed to a first reformer operated at a first set of reaction conditions to generate a first product stream. The first set of reaction conditions includes a first temperature and a first pressure. The second stream is passed to a second reformer operated at a second set of reaction conditions to generate a second product stream. The second set of reaction conditions includes a second temperature and a second pressure. The first pressure is lower than the second pressure. | ||||||
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