| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 101 | Initial hydrotreating of naphthenes with subsequent high temperature reforming | US13327220 | 2011-12-15 | US09079817B2 | 2015-07-14 | 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. | ||||||
| 102 | Process for increasing aromatics production | US13417202 | 2012-03-09 | US08906226B2 | 2014-12-09 | Gregory J. Gajda; Kurt M. VandenBussche; 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 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 utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated. | ||||||
| 103 | Fluid-solid contacting method | US10198197 | 2002-07-17 | US06984311B2 | 2006-01-10 | James W. Kilroy |
| An apparatus and method for contacting fluids in a fluid-solids contacting chamber is disclosed. The fluid-solid contacting chamber has a plurality of beds, and the chamber comprises a plurality of conduits and outlet ports that are capable of providing improved fluid distribution of fluids that are introduced above or between the beds. One or more conduits are arranged within a single conduit, which provides a compact and inexpensive assembly for conveying the fluids to each conduit's outlet port. In operation, the fluid flow to the outlet port of each conduit is regulated within that outlet port's most efficient operating range, and since the flows can regulated simply by hand, the method of this invention can be practiced readily. Catalytic condensation and other hydrocarbon process units that employ this invention will have increased on-stream efficiencies and realize significant economic benefits. | ||||||
| 104 | Reforming with two fixed-bed units, each having a moving-bed tail reactor sharing a common regenerator | US245844 | 1994-05-18 | US5417843A | 1995-05-23 | Gerrit S. Swart; Stuart S. Goldstein; Paul W. Kamienski; George A. Swan, III |
| A process for reforming a gasoline boiling range naphtha stream using a reforming process unit comprised of two independent process units, each of which are operated in two stages. The first stage is operated in a fixed-bed mode and is comprised of a plurality of serially connected fixed bed reactors, and the second stage is operated in a moving bed continuous catalyst regeneration mode. A hydrogen-rich stream is recycled through both stages for each process unit and the moving-bed reforming zones share a common regeneration zone. | ||||||
| 105 | Reformulated-gasoline production | US796519 | 1991-11-21 | US5200059A | 1993-04-06 | 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. The isobutane is processed to yield an ether component by dehydrogenation and etherification. The cracked light naphtha may be upgraded by isomerization. The heavier portion of the cracked 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. The process combination is particularly suited for use in an existing refinery. | ||||||
| 106 | Split-feed naphtha reforming process | US95489 | 1987-09-10 | US4839024A | 1989-06-13 | Michael P. Ramage; Donald C. Wong |
| A naphtha feedstock is reformed by splitting the feedstock into a first C.sub.6 or lower fraction and a C.sub.7 and higher fraction, and passing the C.sub.6 and lower fraction to a reactor and combining the effluent from the first reactor with the C.sub.7 and higher fraction and passing the mixture to a second reactor. The reformate produced has an octane rating at least equivalent to that produced by conventional processes, but has a lowered benzene content. | ||||||
| 107 | Isomerization unit with integrated feed and product separation facilities | US30806 | 1987-03-27 | US4747933A | 1988-05-31 | Frederick M. Hibbs |
| A combination isomerization-reforming process provides additional liquid volume yields of gasoline without significant increase in utilities expense by recycling the isomerization zone effluent to an extended feed fractionation zone from which an isomerization product is also withdrawn. The feed fractionation zone receives a C.sub.5 -plus boiling range naphtha feed. The fractionation zone provides a relatively heavy bottoms stream for a reformer feed and a relatively lighter sidecut stream for feed to an isomerization zone. Effluent from the isomerization zone is recycled to the feed fractionation zone at a midfractionation entry point. A net overhead stream withdrawn from the feed fractionation zone and containing principally C.sub.6 isoparaffins and lighter boiling hydrocarbons provides a relatively high octane blending component. The fractionation zone overhead stream may be combined with effluent from the reforming zone to obtain a gasoline product, at high liquid volume yield, having sufficient octane for unleaded motor fuel use. | ||||||
| 108 | Dual catalyst converter process | US33846773 | 1973-03-06 | US3844934A | 1974-10-29 | BONACCI J; MITCHELL K |
| 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.
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| 109 | Motor fuel production process | US3776837D | 1971-10-20 | US3776837A | 1973-12-04 | DAUTZENBERG F; ALKEMA H |
| HIGH AROMATIC CONTENT MOTOR FUEL IS PRODUCED FROM C5-C8+ NAPHTHA BY SEPARATING THE NAPHTHA INTO A C5-C6 CUT, A SEPARATE C7 CUT AND A C8+ CUT; CATALYTICALLY DEHYDROCYCLIZING THE C7 CUT; CATALYTICALLY REFORMING THE C8+ CUT; AND THEREAFTER COMBINING THE THREE FRACTIONS. IN PREFERRED MODES OF OPERATION, THE C7 CUT IS ALSO SUBJECTED TO CATALYTIC REFORMATION AND THE C5-C6 CUT IS ISOMERIZED BEFORE COMBINATION WITH THE OTHER HYDROCARBON FRACTIONS.
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| 110 | Upgrading wide range gasoline stocks | US3761392D | 1972-05-08 | US3761392A | 1973-09-25 | POLLOCK A |
| A PROCESS FOR UPGRADING WIDE RANGE GASOLINE STOCKS IS DISCLOSED WHEREIN THE FEED IS SEPARATED INTO C5, C6-C8 AND C9+ FRACTIONS, THE C6-C8 AND C9+ FRACTIONS ARE SEPARATELY REFORMED, REFORMATE FROM THE C9+ FRACTION IS DISTILLED TO REMOVE C5-C8 MATERIAL AND YIELD A HEAVY AROMATIC PRODUCT OF HIGH ANTIKNOCK VALUE, SAID C5-C8 MATERIAL IS COMBINED WITH REFORMATE FROM SAID C6-C8 FRACTION AND WITH AROMATIC DEHYDROCYCLIZATE FROM A SUBSEQUENT STEP, THE RESULTING MIXTURE IS EXTRACTED WITH AN AROMATIC-SELECTIVE SOLVENT TO YIELD A RAFFINATE AND C6-C8 AROMATIC PRODUCT OF HIGH PURITY AND ANTIKNOCK VALUE, THE RAFFINATE IS DISTILLED TO OBTAIN A C5-C6 PARAFFINIC FRACTION AND A HEAVY PARAFFINIC FRACTION, THE LATTER IS CATALYTICALLY DEHYDROCYCLIZED TO YIELD SAID AROMATIC DEHYDROCYCLIZATE, THE C5-C6 PARAFFINIC FRACTION IS COMBINED WITH SAID C5 FRACTION AND THE MIXTURE IS CATALYTICALLY ISOMERIZED.
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| 111 | Motor fuel manufacture | US24862638 | 1938-12-30 | US2303663A | 1942-12-01 | SHANKLAND RODNEY V |
| 112 | Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis | US17948718 | 2022-09-20 | US11634648B2 | 2023-04-25 | 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. | ||||||
| 113 | Methods and systems for optimizing mechanical vapor compression and/or thermal vapor compression within multiple-stage processes | US17834339 | 2022-06-07 | US11478724B2 | 2022-10-25 | 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. | ||||||
| 114 | 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. | ||||||
| 115 | 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. | ||||||
| 116 | 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. | ||||||
| 117 | 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. | ||||||
| 118 | 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. | ||||||
| 119 | 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. | ||||||
| 120 | 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. | ||||||
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