| 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 | 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。 | ||||||
| 62 | Processing method of the by-product oil | JP20240588 | 1988-08-13 | JPH0798946B2 | 1995-10-25 | 篤 佐藤; 英幸 土肥; 重信 川上; 圭治 遠藤 |
| 63 | JPS5052104A - | JP9935473 | 1973-09-05 | JPS5052104A | 1975-05-09 | |
| 64 | 벙커C유를 원료유로 하여 윤활조유, 기유 및 아스팔트를 제조하는 방법 | KR1019840005239 | 1984-08-28 | KR100029667B1 | 1989-10-07 | 김주항 |
| 65 | 벙커C유를 원료유로 하여 윤활조유, 기유 및 아스팔트를 제조하는 방법 | KR1019840005239 | 1984-08-28 | KR1019890001185B1 | 1989-04-26 | 김주항 |
| filtering hot water/ bunker oil (1:10) through tungsten net (fitted in coalessor inside) to sep. various inorg. salts, (b) decompression distn. process: using baffle cap as a sieve tray with circulation reflux system of turn down ratio 3.5, (c) dewaxing process: smoothly circulating by liq. ring type vacuum pump (that has nothing to do with slack wax amts.) and (d) redecompression distn. process: maintaining the degree of vacuum in tower top about 150 torr to inlet compressed steam into tower top (to 11 beds) to sep. cut of heavy lub oil to about 360 deg.C. | ||||||
| 66 | 파라핀 및 올레핀의 업그레이드 | KR1020207021216 | 2018-12-12 | KR102342151B1 | 2021-12-23 | |
| 67 | 파라핀 및 올레핀의 업그레이드 | KR1020207021216 | 2018-12-12 | KR1020200101436A | 2020-08-27 | |
| 68 | 벙커C유를 원료유로 하여 윤활조유, 기유 및 아스팔트를 제조하는 방법 | KR1019840005239 | 1984-08-28 | KR1019860001869A | 1986-03-24 | 김주항 |
| 내용없음 | ||||||
| 69 | 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. | ||||||
| 70 | 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. | ||||||
| 71 | 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. | ||||||
| 72 | Dehydrogenation process for gasoline production | US16454513 | 2019-06-27 | US10829702B1 | 2020-11-10 | Rajeswar Gattupalli; Mohamed Shakur; Mark P. Lapinski |
| A process for production of gasoline comprising separating a naphtha feed in a naphtha splitter into a stream comprising i-C5, a stream comprising C6 and lighter boiling hydrocarbons, a C7 stream comprising C7 hydrocarbons, and a heavy stream comprising C8 and heavier hydrocarbons; isomerizing at least a portion of the stream comprising C6 and lighter boiling hydrocarbons in a C5-C6 isomerization zone at isomerization conditions to form a C5-C6 isomerization effluent; dehydrogenating at least a portion of the stream comprising C7 hydrocarbons to form a C7 dehydrogenation effluent comprising C7 olefins; reforming the heavy stream in a reforming zone under reforming conditions forming a reformate stream; and blending one or more of the stream comprising i-C5, the C5-C6 isomerization effluent, the C7 dehydrogenation effluent and the reformate stream to form a gasoline blend. | ||||||
| 73 | Integrated process for production of gasoline | US16049147 | 2018-07-30 | US10294430B1 | 2019-05-21 | Lin Jin; Charles P. Luebke |
| An integrated process for production of gasoline has been described. The process includes a C5-C6 isomerization zone with an associated deisohexanizer, two C7 isomerization zones separated 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 C6 cycloalkanes and heavies from the deisohexanizer are fed to the second C7 isomerization zone to increase the amount of 95 RONC gasoline produced. A higher percentage of 95 RONC gasoline may be achieved by further recycling C6 from deisoheptanizer overhead back to C5-C6 isomerization zone. Higher gasoline yields and higher percentage of 95 RONC gasoline is achieved over the whole naphtha complex with operating costs savings by fully integrating the C5-C6 isomerization zone, two C7 isomerization zones, deisohexanizer and deisoheptanizer columns. | ||||||
| 74 | 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. | ||||||
| 75 | Method of increasing the yield of aviation fuel from renewable feedstocks | US15296987 | 2016-10-18 | US09914880B2 | 2018-03-13 | Geoffrey W. Fichtl; Daniel L. Ellig |
| A method of increasing the yield of renewable aviation fuel is described. A renewable feedstock rich in fatty acids having between 8 and 14 carbon atoms is selected, and the selected feedstock is hydrogenated and deoxygenated in a first reaction zone to provide an effluent rich in normal paraffins having between 9 and 15 carbon atoms. The normal paraffins are isomerized in a second reaction zone to isomerize at least a portion of the normal paraffins. The isomerization reaction mixture may be separated into a product stream comprising a product rich in branched paraffins having between 9 and 15 carbon atoms, which has a higher yield than a product stream made using a renewable feedstock rich in fatty acids having more than 15 carbon atoms. | ||||||
| 76 | 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. | ||||||
| 77 | 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. | ||||||
| 78 | Process for converting FCC naphtha into aromatics | US14309623 | 2014-06-19 | US09434894B2 | 2016-09-06 | Robert Mehlberg; Robert Jason Lee Noe; Antoine Negiz; Steven F. Zink |
| A method and apparatus for processing hydrocarbons are described. The method includes fractionating a hydrocarbon stream to form at least two fractions. The first fraction is reformed to form a reformate stream, and the reformate stream is introduced into an aromatics processing zone to produce aromatic products. At least a portion of the second fraction is cracked in a fluid catalytic cracking unit. A selectively hydrogenated light naphtha stream is formed by separating the cracked hydrocarbon stream into at least two streams and selectively hydrogenating the light naphtha stream, or selectively hydrogenating the cracked hydrocarbon stream and separating the hydrogenated cracked hydrocarbon stream into at least two streams. Aromatics are extracted from the selectively hydrogenated light naphtha stream forming an extract stream and a raffinate stream. The extract stream is hydrotreated, sent to the aromatics processing zone to produce additional aromatic products. | ||||||
| 79 | Distillate fuel blends from Fischer Tropsch products with improved seal swell properties | US09999667 | 2001-10-19 | US06890423B2 | 2005-05-10 | Dennis J. O'Rear |
| The invention provides distillate fuel blend components with improved seal swell and lubricity properties obtained from Fischer Tropsch products. The blends contain a highly paraffinic distillate fuel component and distillate-boiling alkylcycloparaffins and/or distillate-boiling alkylaromatics. The invention further provides processes for obtaining such blends using the products of Fischer Tropsch processes. Finally, the invention provides methods for improving seal swell and lubricity properties for distillate fuels. | ||||||
| 80 | Process for treating by-product oil | US476417 | 1990-04-24 | US5171906A | 1992-12-15 | Shigenobu Kawakami; Keiji Endo; Hideyuki Dohi; Atsushi Sato |
| A process for treating a by-product oil is disclosed, which comprises treating a raw material containing a heavy oil formed as a by-product in the step of producing alkylbenzene or the like by alkylation of benzene or the like, with a catalyst of crystalline synthetic zeolite having a SiO.sub.2 /Al.sub.2 O.sub.3 (molar ratio) of 20 or more and inlets of main pores (main cavity openings) of ten-membered oxygen rings in a liquid phase at a temperature of 320.degree. C. or below, wherein said raw material contains up to 2 wt % of methylnaphthalene. This process makes it possible to prevent reduction in the catalytic treatment efficiency. | ||||||
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