| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 1 | 催化裂化再生催化剂在线转移装置及其系统 | CN96109518.0 | 1996-08-23 | CN1174874A | 1998-03-04 | 石宝珍; 刘献玲; 牛风宾; 张军 |
| 本发明提供了一套固体物料(催化剂)在线转移装置及其系统,由容器(1),容器(2),气控阀(3),计量罐(4)以及与这些设备相连接的管线和阀门所组成的装置,其动力是压缩空气,实现了全气控方式,投用、切断、输送、冷却、计量均用流态化技术,靠气控实现,达到精确计量和自动调节,既可用于高温固体物料,也可用于低温物料。 | ||||||
| 2 | 一种催化裂解的方法及用于实施该方法的设备 | CN202010366580.1 | 2020-04-30 | CN113583705B | 2023-03-10 | 成晓洁; 朱根权; 龚剑洪 |
| 本发明提供一种催化裂解的方法，该方法包括：(1)将富含低碳烷烃的轻烃原料与第一再生催化剂送入第一管状反应器，进行第一催化裂解，得到第一催化裂解后的油剂物料；(2)将第一催化裂解后的油剂物料、重油原料和第二再生催化剂送入第二管状反应器，进行第二催化裂解，得到第二催化裂解后的油剂物料；(3)将第二催化裂解后的油剂物料送入流化床反应器进行第三催化裂解，得到第三催化裂解后的油剂物料；(4)将第三催化裂解后的油剂物料进行油剂分离，得到油气产物和待生催化剂。本公开还提供了一种用于实施如上所述的催化裂解的方法的设备。通过上述技术方案，甲烷和焦炭产率得到了显著地降低，并且同时乙烯和丙烯的产率得到了显著的提高。 | ||||||
| 3 | 一种催化裂解的方法及用于实施该方法的设备 | CN202010366580.1 | 2020-04-30 | CN113583705A | 2021-11-02 | 成晓洁; 朱根权; 龚剑洪 |
| 本发明提供一种催化裂解的方法，该方法包括：(1)将富含低碳烷烃的轻烃原料与第一再生催化剂送入第一管状反应器，进行第一催化裂解，得到第一催化裂解后的油剂物料；(2)将第一催化裂解后的油剂物料、重油原料和第二再生催化剂送入第二管状反应器，进行第二催化裂解，得到第二催化裂解后的油剂物料；(3)将第二催化裂解后的油剂物料送入流化床反应器进行第三催化裂解，得到第三催化裂解后的油剂物料；(4)将第三催化裂解后的油剂物料进行油剂分离，得到油气产物和待生催化剂。本公开还提供了一种用于实施如上所述的催化裂解的方法的设备。通过上述技术方案，甲烷和焦炭产率得到了显著地降低，并且同时乙烯和丙烯的产率得到了显著的提高。 | ||||||
| 4 | 油料气化装置 | CN97206044.8 | 1997-01-31 | CN2281352Y | 1998-05-13 | 张祥杰; 曹新荣; 赵书军 |
| 本实用新型公开了一种油料气化装置,为克服现有技术中的气化装置气化率低的缺点,本实用新型的壳体内设裂解气化器、雾化气化器、搅拌气化器及辅助气化器共四台气化器,本实用新型适于厂矿企业、居民区使用。 | ||||||
| 5 | 一种原料油进料雾化喷嘴及系统 | CN202122722929.3 | 2021-11-08 | CN216173336U | 2022-04-05 | 李章国 |
| 本实用新型公开了一种原料油进料雾化喷嘴及系统，一种原料油进料雾化喷嘴，包括喷嘴本体和位于喷嘴本体一端的喷头；喷嘴本体包括第一套筒和第二套筒，第一套筒的部分插接至第二套筒内，且第一套筒与第二套筒之间留有补气间隙；第一套筒上设有第一进气管和进油管，第二套筒上设有第二进气管。一种原料油进料系统，包括所述的原料油进料雾化喷嘴；所述的原料油进料系统还包括进料设备，进料设备上设有至少一个原料油进料雾化喷嘴。一种原料油进料雾化喷嘴及系统可进行二次进气，二次进气可以进行二次雾化，原料油也就进行了二次破碎，雾化颗粒的直径更小，颗粒的分布也更加均匀，极大提高了破碎效果，对产品收率的提升有明显的促进作用。 | ||||||
| 6 | Heat source for pyrolysis process | US17643044 | 2021-12-07 | US11773335B2 | 2023-10-03 | Brian M. Weiss; Sophie Liu; Michael R. Harper, Jr.; Herbert W. Barry; Changmin Chun; Barrington S. Goldson; Justin R. Johnson; Faria Nusrat |
| Systems and methods are provided for using a reverse flow reactor (or another reactor with flows in opposing directions at different parts of a process cycle) for pyrolysis of hydrocarbons. The systems and methods can include a reactor that includes a combustion catalyst to initiate and/or maintain combustion within the reactor in a controlled manner during the heating and/or regeneration portion(s) of the reaction cycle. A fuel can also be used that has a greater resistance to auto-combustion, such as a fuel that is composed primarily of methane and/or other hydrocarbons. During operation, the temperature in at least an initial portion of the reactor can be maintained at a temperature so that auto-ignition of the auto-combustion resistant fuel injected during the heating step(s) is reduced or minimized. This can allow combustion to be initiated when the auto-combustion resistant fuel comes into contact with the catalyst. Additionally, the amount and positioning of the catalyst within the reactor can be controlled so that combustion of the fuel takes place over a substantially longer period of time than combustion during a conventional reactor heating step. Because the fuel is moving within the reactor during combustion, extending the combustion time results in a substantial expansion of the volume where combustion occurs. Optionally in combination with an improved reaction cycle, this can expand the portion of the reactor that is directly heated by combustion, allowing for an improved temperature distribution within the reactor during the pyrolysis step. | ||||||
| 7 | Apparatus for Heating Regeneration Gas | US11832152 | 2007-08-01 | US20090035191A1 | 2009-02-05 | Keith A. Couch; Xin X. Zhu; James P. Glavin |
| Disclosed is an apparatus for combusting dry gas to heat the air fed to an FCC regenerator to increase its temperature and minimize production of undesirable combustion products. Preferably, the dry gas is a selected FCC product gas. Alternatively or additionally, dry gas from an FCC product stream is separated and delivered to an expander to recover power before combustion. | ||||||
| 8 | Catalytic reforming of hydrocarbons | US56080156 | 1956-01-23 | US2921845A | 1960-01-19 | KYLE ROBERT T; ARVE NILSEN |
| 9 | Refractory regenerative catalytic process | US19563950 | 1950-11-14 | US2846296A | 1958-08-05 | LEONARD HASCHE RUDOLPH |
| 10 | SPENT CATALYST DISTRIBUTOR | EP01990434.1 | 2001-11-21 | EP1352038B1 | 2004-10-13 | CHEN, Ye-Mon; PATEL, Mahendra Sonabhai |
| The present invention is related to methods and apparatus for improving distributions of both spent catalyst and transport gas into a regenerator of a fluid catalytic cracking unit. Spent catalyst and transport gases move upwardly through a spent catalyst riser and are diverted in a radially outward direction by a deflector cone. The catalyst and transport gas are remixed as they move radially outward between two disks before discharging from the outer edges (perimeter) of the distributor into the regenerator in a substantially uniform radial direction. The distributor is adapted to provide continuous discharge from its perimeter so as to cover the entire cross-section of the regenerator. | ||||||
| 11 | HEAT SOURCE FOR PYROLYSIS PROCESS | US17643044 | 2021-12-07 | US20220235282A1 | 2022-07-28 | Brian M. Weiss; Sophie Liu; Michael R. Harper, JR.; Herbert W. Barry; Changmin Chun; Barrington S. Goldson; Justin R. Johnson; Faria Nusrat |
| Systems and methods are provided for using a reverse flow reactor (or another reactor with flows in opposing directions at different parts of a process cycle) for pyrolysis of hydrocarbons. The systems and methods can include a reactor that includes a combustion catalyst to initiate and/or maintain combustion within the reactor in a controlled manner during the heating and/or regeneration portion(s) of the reaction cycle. A fuel can also be used that has a greater resistance to auto-combustion, such as a fuel that is composed primarily of methane and/or other hydrocarbons. During operation, the temperature in at least an initial portion of the reactor can be maintained at a temperature so that auto-ignition of the auto-combustion resistant fuel injected during the heating step(s) is reduced or minimized. This can allow combustion to be initiated when the auto-combustion resistant fuel comes into contact with the catalyst. Additionally, the amount and positioning of the catalyst within the reactor can be controlled so that combustion of the fuel takes place over a substantially longer period of time than combustion during a conventional reactor heating step. Because the fuel is moving within the reactor during combustion, extending the combustion time results in a substantial expansion of the volume where combustion occurs. Optionally in combination with an improved reaction cycle, this can expand the portion of the reactor that is directly heated by combustion, allowing for an improved temperature distribution within the reactor during the pyrolysis step. | ||||||
| 12 | Reverse flow reactors having low maldistribution parameter while containing asymmetric feeds, methods of using same, and pyrolysis products made from same | US17041012 | 2019-04-09 | US11279884B2 | 2022-03-22 | Kevin B. Daly; Federico Barrai |
| Reverse flow reactor (RFR) apparatuses exhibiting asymmetric feed profiles and improved flow distribution during heating mode and/or pyrolysis mode operation, and methods of using same to transform a hydrocarbon feed into a pyrolysed hydrocarbon product are disclosed. The RFR apparatus includes an RFR body with a reaction zone having at least one bed. The RFR body has a central vertical axis and is flanked by first and second void spaces. The method utilizes at least two oxygen-containing feeds, a combustion fuel feed, a purge feed, and a hydrocarbon pyrolysis feed. The RFR apparatus can cycle between an exothermic heating mode (heated to ≥700° C. while maintaining a pressure drop across the reaction zone of ≤100 kPag), a purge mode (purging oxygen using <6 bed volumes of purge gas while maintaining a pressure drop of ≤35 kPag), and an endothermic pyrolysis mode (feeding pyrolysis hydrocarbons through the reaction zone to form pyrolysis products, while maintaining a pressure drop across the reaction zone of ≤70 kPag). | ||||||
| 13 | Process of reforming hydrocarbon-containing gases | US15356261 | 1961-11-20 | US3130020A | 1964-04-21 | ECK JOHN C; GOCZE EDWARD M |
| 14 | Pressure regulation | US45429342 | 1942-08-10 | US2333905A | 1943-11-09 | WATSON CHARLES C |
| 15 | CRACKER MODULAR PROCESSING FACILITY | PCT/US2018/058358 | 2018-10-31 | WO2019089694A1 | 2019-05-09 | HANEY, Fred; DONOVAN, Gary; ROTH, Todd; LOWRIE, Alan; MORLIDGE, George; LUCCHINI, Simon; HALVORSEN, Sean |
The various processes of an ethane cracker plant may be segmented into separate process blocks, which may be interconnected using fluid conduits and/or electrical connections. These process blocks may be directly connected, for example without an external piperack or other external piping interconnecting process blocks. Each process block may be formed of one or more modules The process blocks can include an ethane cracking furnace, a steam generation process, a water stripper, a water quench, a compression, a caustic scrubber, a drier, a deethanizer, an acetylene conversion, a demethanizer, a refrigerator, or a splitter. |
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| 16 | SPENT CATALYST DISTRIBUTOR | PCT/EP2001/013624 | 2001-11-21 | WO02042394A2 | 2002-05-30 | |
| The present invention is related to methods and apparatus for improving distributions of both spent catalyst and transport gas into a regenerator of a fluid catalytic cracking unit. Spent catalyst and transport gases move upwardly through a spent catalyst riser and are diverted in a radially outward direction by a deflector cone. The catalyst and transport gas are remixed as they move radially outward between two disks before discharging from the outer edges (perimeter) of the distributor into the regenerator in a substantially uniform radial direction. The distributor is adapted to provide continuous discharge from its perimeter so as to cover the entire cross-section of the regenerator. | ||||||
| 17 | Process for converting heavy petroleum residues to hydrogen and gaseous distillable hydrocarbons | US699540 | 1985-02-08 | US4609456A | 1986-09-02 | Andre Deschamps; Claude Dezael; Sigismond Franckowiak |
| The invention concerns a process for converting heavy petroleum residues to hydrogen and to gaseous and distillable hydrocarbons, comprising the association of a step of hydropyrolysis (inside tube 3) with a step of catalytic steam-gasification of the formed coke (outside tube 3), characterized in that the hydropyrolysis step is performed in the presence of a solid supporting a carbon gasification catalyst circulating between the hydropyrolysis zone and the coke steam-gasification zone, said steam-gasification being performed in the absence of oxygen.The petroleum residue, hydrogen and steam are introduced respectively through lines 5, 6 and 7.The products are withdrawn through line 10. Heat may be supplied by the radiating tube 4. | ||||||
| 18 | Regenerative hydrocarbon cracking process in series | US26598752 | 1952-01-11 | US2875148A | 1959-02-24 | SCOFIELD RAYMOND C |
| 19 | Hydrocarbon conversion | US40437541 | 1941-07-28 | US2363911A | 1944-11-28 | THOMAS CHARLES L |
| 20 | Catalytic conversion of hydrocarbons | US48822743 | 1943-05-24 | US2363716A | 1944-11-28 | LOUIS WOLK I |
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