| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 121 | METHODS AND SYSTEMS FOR OPTIMIZING MECHANICAL VAPOR COMPRESSION AND/OR THERMAL VAPOR COMPRESSION WITHIN MULTIPLE-STAGE PROCESSES | US17834339 | 2022-06-07 | US20220305398A1 | 2022-09-29 | 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. | ||||||
| 122 | Process for improving the production of benzene and toluene | US16767939 | 2018-11-16 | US11453829B2 | 2022-09-27 | Celine Bertino-Ghera; Alexandre Pagot |
| The invention relates to a process for the production of C6-C7 aromatic compounds from a hydrocarbon feedstock of naphtha type comprising a step of fractionating (2) the feedstock in order to obtain an upper stream and a lower stream, a step of catalytic reforming of the upper stream (6) and of the lower stream (9), a step of recombining (15) the reformate effluents obtained, a step of recontacting (16) and a step of stabilizing (19) the stabilized reformate effluents and a step of separating (22) the raffinate in order to recover C6 and C7 hydrocarbon compounds. | ||||||
| 123 | PROCESSES FOR CONVERTING C2-C5 HYDROCARBONS TO GASOLINE AND DIESEL FUEL BLENDSTOCKS | US17734527 | 2022-05-02 | US20220259121A1 | 2022-08-18 | Chris D'Acosta; Jeffery Miller; Kurtis Sluss |
| 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. | ||||||
| 124 | Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis | US17398594 | 2021-08-10 | US20210371759A1 | 2021-12-02 | 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. | ||||||
| 125 | Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis | US16860638 | 2020-04-28 | US20200255749A1 | 2020-08-13 | 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. | ||||||
| 126 | FUEL COMPOSITION FOR GCI ENGINES AND METHOD OF PRODUCTION | US15872796 | 2018-01-16 | US20180142172A1 | 2018-05-24 | 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. | ||||||
| 127 | Process and installation for the conversion of crude oil to petrochemicals having an improved BTX yield | US14901876 | 2014-06-30 | US09862898B2 | 2018-01-09 | Andrew Mark Ward; Ravichander Narayanaswamy; Vijayanand Rajagopalan; Arno Johannes Maria Oprins; Egidius Jacoba Maria Schaerlaeckens; Raul Velasco Pelaez |
| The present invention relates to an integrated process to convert crude oil into petrochemical products comprising crude oil distillation, reforming, dearomatization, fluid catalytic cracking and aromatic ring opening, which process comprises: subjecting crude oil to crude oil distillation to produce naphtha and one or more of kerosene and gasoil; subjecting naphtha to reforming to produce reformer gasoline; subjecting kerosene and/or gasoil to dearomatization to produce a first stream enriched for alkanes and naphthenes and a second stream enriched for aromatics; subjecting the stream enriched for alkanes and naphthenes to pyrolysis to produce a pyrolysis gasoline or to fluid catalytic cracking to produce a FCC gasoline; subjecting the stream enriched for aromatics to aromatic ring opening to produce a ARO gasoline; and subjecting one or more of reformer gasoline, FCC gasoline and ARO gasoline to gasoline treatment to produce BTX. Furthermore, the present invention relates to a process installation to convert crude oil into petrochemical products using the process of the present invention. The process and the process installation of the present invention have an increased production of petrochemicals at the expense of the production of fuels and an improved BTX yield. | ||||||
| 128 | Power generation from waste heat in integrated aromatics and naphtha block facilities | US15087403 | 2016-03-31 | US09803505B2 | 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. 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. | ||||||
| 129 | Systems for converting ethane and ethanol to liquid transportation fuels | US14571911 | 2014-12-16 | US09545613B2 | 2017-01-17 | Jianhua Yao; Dhananjay Ghonasgi; Tushar Choudhary; Warren Ewert |
| Systems relating to thermal activation (or cracking) of ethane to an intermediate, low purity raw ethylene stream in a first stage. The system then mixes this stream with a stream of raw biomass-derived ethanol that may contain more than four volume percent of water. The resulting mixture is reacted over a suitable catalyst at temperatures and pressures suitable to produce gasoline-range and diesel-range blend stock. | ||||||
| 130 | Maximizing aromatics production from hydrocracked naphtha | US13875506 | 2013-05-02 | US09109169B2 | 2015-08-18 | Fahad Al-Therwi; Noaman Al-Fudail; Mansoor Aleidi |
| A gasoline blending components production system useful for producing both aromatics and gasoline blending components from naphtha. The production system includes a light hydrocracked naphtha splitter, a medium hydrocracked naphtha splitter, a naphtha hydrotreater, an isomerization unit, a continuous catalytic reformer and aromatics complex. The production system is operable to produce both refined benzene and para-xylene products in addition to medium hydrocracked naphtha, isomerate, a C7s cut and a C9+ cut, which are useful for gasoline blending without additional treatment. A method for producing gasoline blending components while maximizing aromatic production includes introducing both stabilized hydrocracked naphtha to the light hydrocracked naphtha splitter and straight run naphtha to the naphtha hydrotreater. Operating the production system produces three types of hydrocracked naphtha: a light hydrocracked naphtha, a medium hydrocracked naphtha and a heavy hydrocracked naphtha. Light and heavy hydrocracked naphtha are directed to the naphtha hydrotreater. | ||||||
| 131 | Process for increasing aromatics production from naphtha | US13416702 | 2012-03-09 | US09102881B2 | 2015-08-11 | Gregory J. Gajda |
| A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process further includes passing one or more catalyst streams through the reformers to optimize selectivity and conversions. | ||||||
| 132 | Integrated hydrogenation/dehydrogenation reactor in a platforming process | US13327178 | 2011-12-15 | US09029618B2 | 2015-05-12 | Manuela Serban; Kurt M. Vanden Bussche; Mark D. Moser; David A. Wegerer |
| A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and partially processing each feedstream in separate reactors. The processing includes passing the light stream to a combination hydrogenation/dehydrogenation reactor. The process reduces the energy by reducing the endothermic properties of intermediate reformed process streams. | ||||||
| 133 | Hydrocarbon conversion | US899219 | 1997-07-23 | US5932777A | 1999-08-03 | Edward L. Sughrue, II; Charles A. Drake; Scott D. Love |
| A hydrocarbon conversion process comprises: (1) contacting a hydrocarbon feed such as, for example, gasoline, with a catalyst under a sufficient condition to effect the conversion of the hydrocarbon to a product stream comprising aromatic hydrocarbons and olefins; (2) separating the product stream into a lights fraction comprising primarily hydrocarbons less than 6 carbon atoms per molecule, a middle fraction comprising C.sub.6 -C.sub.8 aromatic hydrocarbons and non-aromatic hydrocarbons, and a C.sub.9 + fraction comprising aromatic compounds; (3) separating the C.sub.6 -C.sub.8 aromatic hydrocarbons from the middle fraction; and (4) separating hydrocarbons containing 5 or more carbons per molecule (C.sub.5 + hydrocarbons) from the lights fraction. The C.sub.5 + hydrocarbons can be combined with the hydrocarbon feed. The non-aromatic hydrocarbons can also be converted to olefins by a thermal cracking process. Furthermore, the middle fraction can also be obtained by reforming naphtha. | ||||||
| 134 | Production of aliphatic gasoline | US832321 | 1997-03-26 | US5831139A | 1998-11-03 | Robert J. Schmidt; Paula L. Bogdan; Leonid B. Galperin; Jennifer S. Holmgren |
| A process combination is disclosed to selectively upgrade naphtha in accordance with expected trends leading to more-aliphatic gasolines. Such gasolines contain lower concentrations of aromatics and have lower end points with concomitant reduced harmful automotive emissions. The present process combination converts the higher-boiling portion of the naphtha, yields isobutane and other isoparaffins which are particularly suitable for upgrading or blending, and reduces cyclics in intermediate processing steps. | ||||||
| 135 | Gasoline upgrading process | US963229 | 1992-10-19 | US5320742A | 1994-06-14 | David L. Fletcher; Timothy L. Hilbert; David A. Pappal; David W. Rumsey; Gerald J. Teitman |
| A sulfur-containing catalytically cracked naphtha is upgraded to form a low-sulfur gasoline product by a process which retains the octane contribution from the olefinic front end of the naphtha. Initially, the mercaptan sulfur in the front end of the cracked naphtha is converted to higher boiling disulfides by oxidation. The front end, which is then essentially an olefinic, high octane sulfur-free material, may be blended directly into the gasoline pool. The back end, which now contains the original higher boiling sulfur components such as thiophenes, together with the sulfur transferred from the front end as disulfides, is hydrotreated to produce a desulfurized product. This desulfurized product, which has undergone a loss in octane by saturation of olefins, is then treated in a second stage, by contact with a catalyst of acidic functionality, preferably a zeolite such as ZSM-5, under conditions which produce a product in the gasoline boiling range of higher octane value. Because this second product may contain combined organic sulfur, it may be subjected to a final desulfurization to reduce organic sulfur to acceptable levels. | ||||||
| 136 | Process for upgrading naphtha hydrocarbons | US47059 | 1979-06-11 | US4246094A | 1981-01-20 | David A. McCaulay; Thomas D. Nevitt |
| A process which comprises fractionating a wide-boiling range naphtha feedstock into a low-boiling, light-naphtha fraction having an end or maximum boiling point within the range of about 190.degree. to about 200.degree. F. (88.degree. to about 104.degree. C.), and a high-boiling, heavy-naphtha fraction having an initial boiling point within a range of about 190.degree. to about 220.degree. F. (88.degree. to about 104.degree. C.), and contacting the light-naphtha fraction in an isomerization zone with added hydrogen and a catalyst comprising tantalum pentafluoride and hydrogen halide to produce effluent yielding naphthene components which are blended with the heavy-naphtha fraction. The resulting blended material can be processed by reforming to produce an aromatic-rich naphtha product and hydrogen. | ||||||
| 137 | Combination process for upgrading naphtha | US954064 | 1978-10-23 | US4190519A | 1980-02-26 | Stephen J. Miller; Thomas R. Hughes |
| A straight-run naphtha is fractionated at about 66.degree. C., which is just below the boiling point of methylcyclopentane. The 66.degree. C.+ fraction is reformed, and at least a portion of the reformate combined with the 66.degree. C.- fraction and reacted under aromatization conditions over a ZSM-5-type catalyst to form a C.sub.5 + product rich in aromatics. The C.sub.5 + aromaticized product and the remaining reformate can be either sent for BTX recovery or used as a high-octane component of a gasoline blending pool. | ||||||
| 138 | Production of high-octane, unleaded motor fuel | US3787313D | 1972-11-21 | US3787313A | 1974-01-22 | POLLITZER E |
| A naphtha boiling range charge stock is converted into a motor fuel which does not necessitate the incorporation of metalcontaining additives otherwise required for suitable anti-knock characteristics. The process involves a combination of hydrocracking and catalytic reforming, and is effected in a manner which significantly decreases the quantity of methane and ethane produced. The novel form of hydrocracking results in a product predominantly comprising naphthenic hydrocarbons and highly branched paraffins, the latter being predominantly isobutane. Following separation to recover the isobutane, catalytic reforming is utilized to dehydrogenate the naphthenic compounds to produce an aromatic concentrate.
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| 139 | Catalytic reforming proces of selective fractions | US50838455 | 1955-05-16 | US2890994A | 1959-06-16 | DONNELL CONARD K; KENNEDY ROBERT M; ABRAHAM SCHNEIDER |
| 140 | POWER GENERATION FROM WASTE HEAT IN INTEGRATED AROMATICS AND NAPHTHA BLOCK FACILITIES | EP16770106.9 | 2016-08-23 | EP3341574B1 | 2019-05-29 | NOURELDIN, Mahmoud Bahy Mahmoud; AL SAED, Hani Mohammed; BUNAIYAN, Ahmad Saleh |
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