Catalytic reactor with radial distribution of gaseous or liquid feedstock
专利摘要:
The invention relates to a reactor for chemical reactions involving gases or fluids in contact with a solids bed, with essentially radial circulation of these gases or fluids. </ P> <P> This reactor is characterized in that the cylindrical portion of the solids bed is surmounted by a substantially hemispherical reactive zone permeable to gases or fluids. </ P> <P> Application to the catalytic dehydrogenation of hydrocarbons. </ P> 公开号:SU969141A3 申请号:SU772524500 申请日:1977-09-22 公开日:1982-10-23 发明作者:Декуан Даниель;Порте Ален;Ляфон Пьер 申请人:Сосьете Шимик Де Шарбоннаж (Фирма); IPC主号:
专利说明:
The invention relates to a reactor for carrying out chemical reactions and can be used, for example, for carrying out hydrogenation reactions of hydrocarbons, in particular for the production of styrene from ethylbenzene. Known catalytic reactor with a radial distribution of gaseous or liquid feed containing. a thick catalyst layer enclosed between two perforated cylinders and an additional gas-permeable section with a catalyst located on the layer (1]. A disadvantage of the known reactor is that during operation there is a gradual compaction of the solid layer. To compensate for this seal and to be able to maintain the required radial circulation. in the reactor, an excess amount of solids must be introduced into the upper part of the reactor. However, the indicated upper part is gradually contaminated, since it is not blown with gases and is not washed with the liquids involved in the reaction. The purpose of the invention is to increase the efficiency of the reactor by improving the distribution. To achieve this goal, a layer containing a layer in a catalytic reactor with a radial distribution of gaseous or liquid raw materials. the catalyst, enclosed between two perforated cylinders, is a full-blown gas-permeable section with a catalyst located on the layer, made in the form of a hemisphere. . Moreover, based on the manufacturability of the design, it can also be made in the form of a cylinder or a truncated cone that fit into the ball. In the reactor, the circulation of gases or liquids may * be centrifugal 965 or centripetal. Is centripetal preference given circulation. The outflow resistance of products in such a reactor increases as they move toward the center of the reactor. Therefore, in the peripheral part of the layer, the pressure loss per unit length is insignificant, but it increases significantly in the part of the reactor adjacent to the center. Therefore, the decrease in the level of the solid layer in the upper part of the reactor caused by shrinkage has a very small effect on the pressure loss and, therefore, has little effect on the circulation of gases or liquids in the reaction mass. Figure 1 shows a reactor, a vertical section; in FIG. 2 - node I in figure 1. The reactor contains a housing 1, inside of which a perforated outer shell 2 and a central pipe 3 are coaxially mounted. Above the central pipe 3 are two truncated cones 4 and 5, which form a substantially hemispherical shape zone. Perforated holes made in tube 3 make up 8% of its surface (pressure loss is about 5 g / cm 2 ), whereas perforated holes made in truncated cones 4 and 5 make up about 16% of their surface (pressure loss approximately 1 g / cm 2 ). 35 Above the perforated outer shell 2 has two perforated truncated cone 6 and 7 · perforated holes formed in the shell, it is 3% po- surface 40 (the head loss is about 8 g / cm 2). Perforated holes made in cones 6 and 7 occupy about 3% of their surface (pressure loss is about 45 g / cm 2 ). The mass of the catalyst is- '' separated from sheets 2 and 3 by two metal grids 8 and 9. The first grid 8 with large cells is superimposed on the perforated sheet from the side - 5® of the catalytic layer, allowing ga141 4 to be distributed between the perforated holes made in the sheet, and the second mesh 9 with small cells is superimposed on the first mesh 5 and holds the catalytic layer and prevents clogging of the perforated holes. The mass of the catalyst is placed on the carrier 10, which is designed so that it does not interfere with the free expansion of the reactor. The centering elements 11 provide the desired position of the catalyst mass. Catalytic reactor operates as follows. 1 Superheated reaction gases are introduced into the reactor through the nozzle 12. A cone 13 made of a perforated sheet ensures the distribution of gases in the empty peripheral space 14 before they enter the catalytic mass. Passing through the catalyst gases are cooled, the reaction de25 hydrogenation is endothermic, and then they reach the central tube 3 and exit through nozzle 15 'in the reactor are provided nozzles 16 for removal of the catalyst, external · 30' insulating coating 17, as well as elements 18 connect the metering means temperature and pressure.
权利要求:
Claims (1) [1] 3 or centripetal. Centripetal circulation is preferred. Resistance to product outflow in such a reactor increases as they move to the center of the reactor. Therefore, in the peripheral part of the layer, the loss of head pressure per unit length is insignificant, but it significantly increases in the part of the reactor adjacent to the center. There is little effect on the circulation of gases or liquids in the reaction mass. Figure 1 shows the reactor, a vertical section; figure 2 - node I in figure 1. The reactor includes a housing 1, inside of which perforated outer shell 2 and central pipe 3 are coaxially mounted. Two truncated cones 4 and 5 are located above the central pipe 3, forming a zone of a completely hemispherical shape. The perforated holes made in the pipe 3 comprise 8 of its surface (the pressure loss is about 5 g / cm 2), such as the perforated holes made in truncated cones and 5 are about I6t from their surface (the pressure loss is about 1 g / cm). Above the outer perforated gull 2, two truncated perforated cones 6 and 7 are installed. The perforated holes made in the shell are 3% of its surface (head loss is about 8 g / cm). The perforated holes, made in the cones 6 and 7, occupy about 3% of their surface (the pressure loss is about 5 g / cm). The mass of the catalyst is separated from sheets 2 and 3 by two metal grids 8 and 9. The first grid 8 with large cells is superimposed on the perforated sheet from the side of the catalytic bed, which allows the jack to be distributed between the perforated holes made in the sheet, and the second grid 9 with small cells, it is superimposed on the first grid and holds the catalytic layer and prevents clogging of perforated holes. The mass of the catalyst is placed on a carrier 10, which is designed so that it does not prevent the free expansion of the reactor. The price of the grinding elements 11 provide the desired position of the mass of the catalyst. The catalytic reactor operates as follows. Overheated reaction gases are introduced into the reactor through nozzle 12. A cone 13 made of a perforated sheet provides for the distribution of gases in the empty peripheral space And before they enter the catalytic mass. The passage through the catalyst is cooled, the dehydrogenation reaction is endothermic, then it reaches the central tube 3 and exits through the nozzle 15. The nozzles 16 are provided in the reactor to remove the cat dispenser, the outer insulation coating 17 temperature and pressure measurements. Claims of the Invention — A catalytic reactor with radial distribution of a gaseous or liquid raw material, comprising an atalizer layer sandwiched between two perforated cylinders and an additional gas-permeable section with a catalyst located on the bed, in order to increase the reactor efficiency by improving distribution, the additional section with the catalyst is made in the form of a hemisphere. Sources of information taken into account in the examination 1. US Patent No. 299737, cl. 23-288, 1961. 12 15 2
类似技术:
公开号 | 公开日 | 专利标题 US4127389A|1978-11-28|Exchanger reactor JP2635283B2|1997-07-30|Catalyst reactor bed US4033727A|1977-07-05|Separator ring in fixed bed radial flow catalytic reactor US4374094A|1983-02-15|Method and apparatus for uniform flow through radial reactor centerpipes US3694169A|1972-09-26|Low pressure-drop catalytic reactor US4820495A|1989-04-11|Plate reactors for chemical syntheses under high pressure in gaseous phase and with heterogeneous catalysis US3723072A|1973-03-27|Fluid contacting apparatus KR890002150B1|1989-06-21|Multiple stage reactor system for a moving catalyst bed SU969141A3|1982-10-23|Catalytic reactor with radial distribution of gaseous or liquid feedstock EA022045B1|2015-10-30|Process for conversion of synthesis gas to higher hydrocarbons | KR20140001590U|2014-03-17|Heat exchange reactor US4647549A|1987-03-03|Regeneration of hydrocarbon conversion catalyst US4357304A|1982-11-02|Moving catalyst bed reactor EP0841317B1|2002-01-09|Process for dehydrogenation of ethylbenzene to styrene US2548519A|1951-04-10|Apparatus for conducting high-temperature reactions US4411870A|1983-10-25|Reactor system US4832921A|1989-05-23|Apparatus for regeneration of hydrocarbon conversion catalyst US2385189A|1945-09-18|Catalytic reactor US4411869A|1983-10-25|Multiple stage reactor system US3948610A|1976-04-06|Catalyst beds for oxidizing ammonia to nitrogen oxides JPH11285631A|1999-10-19|In si-tu-modernizing method of heterogeneous synthetic reaction device and heterogeneous synthetic reaction device RU188296U1|2019-04-05|REACTOR RU2002131458A|2004-03-27|CATALYTIC REACTOR FOR EXOTHERMAL PROCESSES PROCESSING IN A GAS-SOLID PHASE WITH A DIFFERENT TEMPERATURE DIFFERENCE US1910365A|1933-05-23|Method for effecting catalytic exothermic gaseous reactions US2310962A|1943-02-16|Contact treatment of fluids
同族专利:
公开号 | 公开日 AT361901B|1981-04-10| NO147135B|1982-11-01| DK149604B|1986-08-11| ATA674677A|1980-09-15| FR2365370A1|1978-04-21| NO147135C|1983-02-09| PT67055A|1977-10-01| US4169879A|1979-10-02| PT67055B|1979-02-19| SE428178B|1983-06-13| FI772779A|1978-03-23| FI65380C|1984-05-10| SE7710597L|1978-03-23| CS235065B2|1985-04-16| DE2742752A1|1978-03-30| FR2365370B1|1979-01-12| DK149604C|1987-01-05| MX145412A|1982-02-04| FI65380B|1984-01-31| DE2742752C2|1991-06-27| NO773248L|1978-03-28| DK418677A|1978-03-23|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题 RU2654041C2|2013-01-30|2018-05-15|Чайна Петролеум Энд Кемикал Корпорейшн|Premixing device, reactor with fixed bed and radial flow and reaction system for oxidative dehydrogenization of butylene|US2639224A|1950-08-31|1953-05-19|Gulf Oil Corp|Catalytic reactor| US2635989A|1950-08-31|1953-04-21|Gulf Oil Corp|Catalytic process and apparatus| US2886517A|1954-05-06|1959-05-12|Kellogg M W Co|Method and apparatus for catalytic reactions| US2969318A|1956-12-17|1961-01-24|Texaco Inc|Spent catalyst seal for a catalytic reactor| US2997374A|1958-03-13|1961-08-22|California Research Corp|Radial flow reactor| US3027244A|1959-02-09|1962-03-27|Union Oil Co|Radial flow catalytic reactor| US3051561A|1959-05-14|1962-08-28|Standard Oil Co|Radial flow reactor| US3211537A|1960-04-11|1965-10-12|Phillips Petroleum Co|Fluid-solids contacting| US3167399A|1962-05-08|1965-01-26|Universal Oil Prod Co|Radial flow reactor| US3235343A|1962-09-11|1966-02-15|Phillips Petroleum Co|Removal of scale or other entrained solids from fluid to be treated| US3515763A|1968-04-22|1970-06-02|Universal Oil Prod Co|Production of styrene|US4705621A|1985-03-22|1987-11-10|Mobil Oil Corporation|Catalytic reactor system with crosscurrent liquid and gasflow| CH670400A5|1986-03-13|1989-06-15|Ammonia Casale Sa| DE19735389C1|1997-08-14|1998-09-03|Linde Ag|Chemical reactor for adsorptive separation processes has upright cylindrical mantle| DE19735397A1|1997-08-14|1998-09-24|Linde Ag|Reactor for the adsorptive separation of a gas mixture| US6245303B1|1998-01-14|2001-06-12|Arthur D. Little, Inc.|Reactor for producing hydrogen from hydrocarbon fuels| US6296814B1|1998-11-10|2001-10-02|International Fuel Cells, L.L.C.|Hydrocarbon fuel gas reformer assembly for a fuel cell power plant| DE102008010422A1|2008-02-21|2009-09-03|Uhde Gmbh|Fixing device for catalyst particles| US8759600B2|2010-06-28|2014-06-24|Uop Llc|Reduced fluidization of solid particles in radial flow fluid/solid contacting|
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申请号 | 申请日 | 专利标题 FR7628540A|FR2365370B1|1976-09-22|1976-09-22| 相关专利
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