| 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 | Gasoline upgrading process | US913326 | 1992-07-15 | US5413697A | 1995-05-09 | David L. Fletcher; Michael S. Sarli; Stuart S. Shih |
| 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 containing, preferably an intermediate pore size zeolite such as ZSM-5 and a zeolite such as MCM-22. 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. | ||||||
| 122 | Gasoline upgrading process | US891124 | 1992-06-01 | US5413696A | 1995-05-09 | David L. Fletcher; Timothy L. Hilbert; Stephen J. McGovern; Michel S. Sarli; Stuart S. Shih |
| 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 comprising zeolite beta. 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. | ||||||
| 123 | Gasoline upgrading process | US891248 | 1992-06-01 | US5407559A | 1995-04-18 | Thomas F. Degnan; Stuart S. Shih |
| A process is provided for producing low sulfur gasoline of relatively high octane number from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by treatment over an acidic catalyst comprising crystals having the structure of ZSM-12. The treatment over the acidic catalyst comprising ZSM-12 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. | ||||||
| 124 | Gasoline upgrading process | US929543 | 1992-08-13 | US5326462A | 1994-07-05 | Stuart S-S. Shih; Kathleen M. Keville; Daria N. Lissy |
| 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 system comprising a zeolite having the topology of ZSM-5 and a zeolite sorbing 10 to 40 mg 3-methylpentane at 90.degree. C., 90 torr, per gram dry zeolite in the hydrogen form, e.g., ZSM-22, ZSM-23, or ZSM-35. The treatment over the acidic catalyst system 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. | ||||||
| 125 | Process for improving the hydrogen donor properties of a coal liquefaction solvent | US478196 | 1983-03-24 | US4476009A | 1984-10-09 | Erven J. Kuhlmann; Richard P. Guptill; Dick Y. Jung; Hyung K. Zang |
| A process for improving the properties of a hydrogen donor coal liquefaction solvent employed in a coal liquefaction process which comprises separating said coal liquefaction solvent into a first fraction boiling in the range from about 350.degree. to about 675.degree. F., and a second fraction boiling in the range from about 675.degree. F. to about 1000.degree. F., hydrogenating said first fraction at a temperature ranging from about 600.degree. to about 800.degree. F., under a pressure of about 500 to 4000 psig, hydrogenating said second fraction at a temperature ranging from about 600.degree. to 700.degree. F. at a pressure from about 500 to 4000 psig and combining said hydrogenated first and second fractions to provide a coal liquefaction solvent having an increased concentration of hydrogen donor components. | ||||||
| 126 | Removing H.sub.2 S from gas with recycled NMP extraction solvent | US973680 | 1978-12-27 | US4208382A | 1980-06-17 | John H. Blume; James D. Bushnell; Milton D. Leighton |
| An improved process for removing H.sub.2 S from a hydrofiner tail gas wherein said tail gas is passed into a scrubbing zone wherein it is contacted with liquid NMP to remove most of the H.sub.2 S from the gas to form an H.sub.2 S-rich NMP solution and the H.sub.2 S-rich NMP solution is heated and passed into a stripping zone to remove most of the H.sub.2 S from the NMP to form an H.sub.2 S-lean NMP solution, extracting a hydrocarbon oil with an NMP solution, recovering hot liquid, NMP from said extracted oil and combining it with said H.sub.2 S-lean NMP solution and wherein said combined solution comprises at least a portion of said NMP solution used to extract said oil, wherein the improvement comprises heating the H.sub.2 S-rich NMP solution to the required stripping temperature by indirectly contacting same, in heat exchange relationship, with at least a portion of said combined NMP solution.This process is especially useful for scrubbing H.sub.2 S from hydrofiner tail gas for use as once-through stripping gas in the solvent recovery section of a lube oil extraction process employing NMP as the extraction solvent, and in a preferred embodiment, the spent stripping gas from the lube oil solvent recovery is used as the stripping gas in the stripping zone of this invention. | ||||||
| 127 | Electrical insulating oils | US636391 | 1975-12-01 | US4033854A | 1977-07-05 | Tadashi Ohmori; Tokuo Fujisou |
| An electrical insulating oil having excellent oxidation stability, thermal stability and/or hydrogen absorbability consisting essentially of (A) a base hydrocarbon oil obtained by hydrofining and then dewaxing a fraction boiling at 280.degree.-400.degree. derived from a paraffin or mixed base crude oil, (B) a highly aromatic hydrocarbon oil obtained by hydrofining and/or distilling a heavy hydrocarbon fraction boiling at 250.degree.-400.degree. C produced as a by-product at the time of catalytically reforming naphtha or the like and, if desired, (C) an oil obtained by treating a lubricating oil fraction boiling at 230.degree.-500.degree. C derived from a crude petroleum oil. | ||||||
| 128 | Systems and processes for processing pyrolysis oil | US18054169 | 2022-11-10 | US11802250B1 | 2023-10-31 | Bruce D. Murray; Scott G. Morrison; Kenneth Fountain; Steven R. Horlacher; Vincent D. Mcgahee; Reza Khankal; David Dockter |
| A system for processing plastic waste may include a feed line, a feed fractionator, a hydrotreater, a catalytic reforming unit, a heavy oil cracker, and a steam cracker. A pyrolyzed plastics feed is separated into light, medium, and heavy hydrocarbon streams. The hydrotreater removes sulfur, and the catalytic reforming unit produces a circular aromatic-rich stream. The heavy oil cracker generates cracked streams. The steam cracker produces a circular olefin stream from a cracked stream. A system for processing plastic waste may include the feed line, the feed fractionator, the hydrotreater, a medium hydrocarbon fractionator, the catalytic reforming unit, a full-range reforming unit, the heavy oil cracker, and the steam cracker. The medium hydrocarbon fractionator produces two hydrocarbon streams. The full-range naphtha reforming unit produces a second circular aromatic-rich stream. | ||||||
| 129 | Integrated process and system for treatment of hydrocarbon feedstocks using deasphalting solvent | US16840386 | 2020-04-04 | US11384298B2 | 2022-07-12 | Omer Refa Koseoglu |
| Separation of asphaltenes from residual oil is carried out with naphtha as solvent. In particular, straight run naphtha obtained from the same crude oil source as the residual oil feed is used as the solvent. The mixture of deasphalted oil and solvent is passed to a hydroprocessing zone, without typical separation and recycle of the solvent back to the solvent deasphalting unit. Asphalt is separated from the residual oil (residue from atmospheric or vacuum distillation); the mixture of deasphalted oil and naphtha solvent is passed to the hydroprocessing unit. | ||||||
| 130 | Polished turbine fuel | US16089850 | 2016-10-18 | US10683461B2 | 2020-06-16 | Mohammed Wohaibi; Tom F. Pruitt |
| Turbine fuel provided for large-scale land based turbines used by utilities for producing electricity and desalinated water, and for large mobile engines and turbines in marine and remote applications where only liquid fuels are available. Use results in less corrosion, ash formation and emissions (NOx, SOx, CO2 and noxious metals) than firing contaminated heavy crude, refinery residual oils or high sulfur fuel oils. Manufacture is by decontaminating crude oils, non-conventional crudes, and other highly contaminated feeds. Each fuel is produced as a single product of unit operations, not ex-plant blend of various refinery products, yet using an apparatus configuration less complex than conventional crude oil refining. These fuels can be fired by advanced high efficiency turbines of combined cycle power plants having hot flow paths and heat recovery steam generation systems susceptible to corrosion, which systems cannot otherwise risk contaminated heavy crudes or refinery residual oils feeds. | ||||||
| 131 | POLISHED TURBINE FUEL | US16780463 | 2020-02-03 | US20200172820A1 | 2020-06-04 | Mohammed Wohaibi; Tom F. Pruitt |
| Turbine fuel provided for large-scale land based turbines used by utilities for producing electricity and desalinated water, and for large mobile engines and turbines in marine and remote applications where only liquid fuels are available. Use results in less corrosion, ash formation and emissions (NOx, SOx, CO2 and noxious metals) than firing contaminated heavy crude, refinery residual oils or high sulfur fuel oils. Manufacture is by decontaminating crude oils, non-conventional crudes, and other highly contaminated feeds. Each fuel is produced as a single product of unit operations, not ex-plant blend of various refinery products, yet using an apparatus configuration less complex than conventional crude oil refining. These fuels can be fired by advanced high efficiency turbines of combined cycle power plants having hot flow paths and heat recovery steam generation systems susceptible to corrosion, which systems cannot otherwise risk contaminated heavy crudes or refinery residual oils feeds. | ||||||
| 132 | Integrated isomerization and hydrotreating apparatus | US16156393 | 2018-10-10 | US10351785B2 | 2019-07-16 | Omer Refa Koseoglu |
| Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by with an apparatus arranged for flashing the feed at a target cut point temperature to obtain two fractions. A low boiling temperature fraction contains refractory, sterically hindered sulfur-containing compounds, which have a boiling point at or above the target cut point temperature. A high boiling temperature fraction, having a boiling point below the target cut point temperature, is substantially free of refractory sulfur-containing compounds. The high boiling temperature fraction is contacted with isomerization catalyst, and the isomerized effluent and the low boiling temperature fraction are combined and contacted with a hydrotreating catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level. | ||||||
| 133 | INTEGRATED ISOMERIZATION AND HYDROTREATING APPARATUS | US16156393 | 2018-10-10 | US20190071609A1 | 2019-03-07 | Omer Refa KOSEOGLU |
| Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by with an apparatus arranged for flashing the feed at a target cut point temperature to obtain two fractions. A low boiling temperature fraction contains refractory, sterically hindered sulfur-containing compounds, which have a boiling point at or above the target cut point temperature. A high boiling temperature fraction, having a boiling point below the target cut point temperature, is substantially free of refractory sulfur-containing compounds. The high boiling temperature fraction is contacted with isomerization catalyst, and the isomerized effluent and the low boiling temperature fraction are combined and contacted with a hydrotreating catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level. | ||||||
| 134 | Adsorbent for desulfurization of gasoline and method for desulfurization of gasoline | US14931690 | 2015-11-03 | US10011779B2 | 2018-07-03 | Liang Zhao; Jinsen Gao; Chunming Xu; Tianzhen Hao; Xiaona Han |
| The present invention provides an adsorbent and a method for desulfurization of gasoline. The adsorbent is obtained by loading active metal component on a composite carrier comprising zeolite and active carbon subjected to alkali treatment respectively, the active metal is selected from one or more elements of IA, IIA, VIII, IB, IIB and VIB groups in the periodic table. This method uses the adsorbent to conduct gasoline adsorption desulfurization, which especially cuts the gasoline into a light and a heavy gasoline fraction firstly, then the light fraction is subjected to adsorption desulfurization using the adsorbent, and the heavy fraction is subjected to selective hydrodesulfurization, a cutting temperature of the light and the heavy gasoline fraction is 70-110° C. The adsorbent has a large sulfur adsorption, a long service life, and simply to be regenerated; the method can realize deep desulfurization of gasoline, and has a less octane number loss. | ||||||
| 135 | PROCESS AND SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM RESIDUE HYDROPROCESSING | US15817133 | 2017-11-17 | US20180155641A1 | 2018-06-07 | Mohammed Saeed AL-GHAMDI; Bader BaHammam; Naif AL OSAIMI; Sami BARNAWI |
| Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include gas oil range intermediates from the vacuum gas oil hydroprocessing zone and the vacuum residue hydrocracking zone. | ||||||
| 136 | Process of hydroconversion-distillation of heavy and/or extra-heavy crude oils | US13598684 | 2012-08-30 | US09920264B2 | 2018-03-20 | Jorge Ancheyta Juarez; Jose Antonio Domingo Muñoz Moya; Luis Carlos Castañeda Lopez; Sergio Ramirez Amador; Gustavo Jesus Marroquin Sanchez; Guillermo Centeno Nolasco; Fernando Alonso Martinez; Rodolfo Antonio Aguilar Escalante |
| A process for hydroconversion-distillation of heavy and/or extra-heavy crude oils, which comprises four stages: 1) desalting and separation of the feedstock; 2) catalytic hydrotreating of light fraction (optional); 3) catalytic hydroconversion of heavy fraction, and 4) distillation of hydrotreated products to provide products that can be processed in conventional refining schemes designed to operate with light and intermediate crude oils. | ||||||
| 137 | Integrated process for in-situ organic peroxide production and oxidative heteroatom conversion | US14679495 | 2015-04-06 | US09909074B2 | 2018-03-06 | Omer Refa Koseoglu; Abdennour Bourane |
| An oxidative treatment process, e.g., oxidative desulfurization or denitrification, is provided in which the oxidant is produced in-situ using an aromatic-rich portion of the original liquid hydrocarbon feedstock. The process reduces or replaces the need for the separate introduction of liquid oxidants such as hydrogen peroxide, organic peroxide and organic hydroperoxide in an oxidative treatment process. | ||||||
| 138 | Process for deeply desulfurizing catalytic cracking gasoline | US14684196 | 2015-04-10 | US09856423B2 | 2018-01-02 | Tianzhen Hao; Jinsen Gao; Dezhong Li; Liang Zhao; Zhiyuan Lu; Xingying Lan |
| The present invention provides a process for desulfurizing gasoline fraction by solvent extraction: introducing the gasoline fraction into an extraction tower at a lower-middle part thereof, introducing a solvent into the extraction tower at the top thereof, injecting saturated C5 hydrocarbon into a reflux device at the bottom of the extraction tower, wherein the gasoline fraction which is desulfurized flows out from the top of the extraction tower; the solvent that has extracted sulfide, aromatics and C5 hydrocarbon flows out from the bottom of the extraction tower, and is separated into a C5 hydrocarbon-containing light component, a sulfur-rich component, water and the solvent. The present invention also provides a process for deeply desulfurizing catalytic cracking gasoline, which flexibly combines the process described above and an existing desulfurization technology. | ||||||
| 139 | Integrated system for in-situ organic peroxide production and oxidative heteroatom conversion and hydrotreating | US14679523 | 2015-04-06 | US09637690B2 | 2017-05-02 | Omer Refa Koseoglu; Abdennour Bourane |
| An oxidative treatment system, e.g., oxidative desulfurization or denitrification, is provided in which the oxidant is produced in-situ using an aromatic-rich portion of the original liquid hydrocarbon feedstock. The process reduces or replaces the need for the separate introduction of liquid oxidants such as hydrogen peroxide, organic peroxide and organic hydroperoxide in an oxidative treatment process. | ||||||
| 140 | Method for producing hydrocarbon oil and system for producing hydrocarbon oil | US13817182 | 2011-08-12 | US09493714B2 | 2016-11-15 | Kazuhiko Tasaka; Yuichi Tanaka; Marie Iwama |
| Hydrocarbon oil obtained by Fischer-Tropsch (FT) synthesis reaction using a catalyst within a slurry bed reactor is fractionated into a distilled oil and a column bottom oil in a rectifying column, part of the column bottom oil is flowed into a first transfer line that connects a column bottom of the rectifying column to a hydrocracker, at least part of the column bottom oil is flowed into a second transfer line branched from the first transfer line and connected to the first transfer line downstream of the branching point, the amount of the catalyst fine powder to be captured is monitored while the catalyst fine powder in the column bottom oil that flows in the second transfer line are captured by a detachable filter provided in the second transfer line, and the column bottom oil is hydrocracked within the hydrocracker. | ||||||
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