• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Process for contacting particulate solids (e.g. cracking catalyst) with a fluid (e.g. a hydrocarbons-comprising mixture) by introducing said fluid as a, preferably single, annular stream into a stream comprising the particulate solids. The invention further relates to an apparatus for contacting particulate solids with a fluid comprising a solids container (e.g. a fluid catalytic cracking riser reactor) at least partly surrounding fluid supply means which have an inlet opening in the upstream end part and an annular fluid outlet opening in the downstream end part thereof.
    公开号:SU1551240A3
    申请号:SU874202210
    申请日:1987-03-25
    公开日:1990-03-15
    发明作者:Хэддон Барнс Питер
    申请人:Шелл Интернэшнл, Рисерч Маатсхаппий Бв (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to devices for forming contact between solid particles and a liquid, especially between catalyst particles and a hydrocarbon oil product stream in the lower part of the reaction apparatus of a liquid catalytic cracking unit (FOC).
    The aim of the invention is to increase the efficiency of the process.
    FIG. 1 shows a device for the interaction of solid particles with a liquid, longitudinal section; in fig. 2 - the lower part of the reaction apparatus of a liquid catalytic cracking stand, longitudinal section; in fig. 3 is a section A-A in FIG. one; in fig. 4 is a section BB in FIG. 2
    The device contains a pipe 1 of the fluid, large (downstream)
    a part of which is surrounded by the lower part of the body 2 of the device for solid particles. The end portion 3 of the fluid supply pipe 1 preferably comprises a separate inlet means 4 for the first fluid and more preferably a tubular inlet means 5 for the second fluid partially located inside the end portion 3. In the embodiment shown in FIG. 1, the annular inlet 6 is 6 the first fluid is formed between the wall of the fluid supply pipe 1 and the tubular inlet means 5 in order to accelerate the upward flow (along the flow) of the first fluid and ensure its distribution over the cross section You pipe 1 supply of fluid. Further acceleration and mixing of the first and second fluids can be achieved by
    SP
    using a liquid supply pipe 1, the cross-sectional area of which decreases in the downstream direction. The preferred ratio of the diameters in the flow of the ends of the outlets 3 and 7 of the pipe 1 of the liquid supply is 1-5, and the most preferred is 1.2-3. .
    The main advantage of the proposed device is that the liquid supply pipe 1 is located in the center of the lower part 8 of the solid body 2 can be used to achieve rapid and homogeneous mixing of the solid particles with the liquid.
    The end portion 9 of the tubular inlet means 5 may comprise installation means, for example, outwardly directed spacing ribs 10. In the end portion 9 there are at least one hole 11. However, in some cases it is advantageous to have several holes in the end portion 9, the second liquid stream flows at a relatively high speed (for example, 30-300 m / s) and, accordingly, the velocity of the living-room mixture flowing through the pipe 1 of the fluid yearn increases. In a preferred implementation warrant in the hole 11 y tanavlivaets reflector which defines an annular fluid opening. The reflector may contain a rotating symmetrical body with an increasing diameter in the direction of flow;
    An annular fluid outlet 12 is preferably formed between the wall (downstream), the end part 7 of the fluid supply pipe 1 and the reflector 13. The rotating symmetric body with increasing diameter downstream is a conical body with an opening angle in the range of 10-1800, preferably 80 -120 ° "The ratio of the base diameter of this conical body and the diameter of the end part 7 of the liquid supply pipe 1 is preferably 0.8-6, most preferably 1-4. The reflector 13 can be held in place by the connecting means 14, which can be installed inside or outside (Fig. 1) of the end part 7 of the pipe 1, in the latter case the connecting means 14 can also serve as
    Q
    n 5 35
    50 55
    0
    blades inside the annular opening 15 formed between the tubular protective means 16 and the end part 7 of the pipe 1. The rod 17 can be installed coaxially inside the liquid supply pipe 1 and connected to the reflector 13 to achieve a stable annular liquid flow around the rod.
    The proposed device contains a distribution device 18, for example, in the form of a perforated plate (Fig. 1) or an annular bubbler having uniformly spaced apertures, for example, nozzles 19, through which fluidized gas (for example, flow or waste acid-catalytic cracking gas, introduced through inlet means 20, enters mixing zone 21. In addition, a separate stream of gas introduced through the inlet means 22 can be used to cool the space 23 between the protective means 16 and the pipe 1. The solid body 2 can contain a section with a narrowed diameter (not shown) near the annular liquid outlet 15 to increase velocity of the fluidized bed of solid particles surrounding this hole, which improves the contact between the liquid (mixture) coming from the liquid outlet 15 with solid particles.
    FIG. Figure 2 shows another embodiment of a device that is used as part of a device for liquid catalytic removal of hydrocarbon substances.
    The device further comprises an inlet means 24 for introducing solid particles (e.g., coming from a catalyst regenerator) into the lower section of housing 2, which may be a reaction apparatus of a stand of a liquid catalytic cracking device. A cooling gas, such as low pressure steam, may be introduced through the cooling gas inlet means 22 and the cooling gas inlet space 25 into the space 23 enclosed between the walls of the lower section 26 of the safety means 16 and removed through the annular opening 15, in which blades 27. The crude oil product is introduced through inlet means 5 and four.
    cutting a hole 11 in the lower (downstream) end portion 9 into the liquid supply pipe 1, where, mixing with steam introduced through the input means 4 takes place.
    Example. The feed flow of heavy oil enters the input means 5 of the device, as shown in FIG. 2, at 250 ° С and pressure of 12 bar abs. and is mixed in the liquid supply pipe 1 with a length of 3 m and a diameter of 0.2 m with steam introduced through the inlet means 4 at 300 ° C and a pressure of 15 bar abs. The mixture of oil product and steam flows at a speed of 50 m / s through the annular outlet 12 to the mixing zone 21, which operates at a pressure of 3 bar abs. and 520 ° C. The regenerated silica-alumina catalyst in powder form is introduced through inlet means 24 at 700 ° C to the mixing zone 21, where the catalyst particles come into contact with the mixture of oil and steam.
    The use of a solids injection device, which is centrally located in the lower section of the reaction apparatus of the effluent, as shown in Figure 2, allows uniform mixing of the solid cracking catalyst and the liquid (hydrocarbon and steam) in the mixing zone 21 in a relatively short period of time. therefore, the length of the section of the reaction vessel, in which the particles of the solid catalyst are mixed with the hydrocarbon feed, is relatively small, as well as the optimal use of the rest (upper) section riser reaction apparatus for catalytic cracking
    512406
    In addition, when using the proposed device, only a relatively small amount of steam or other liquid is consumed for 5 injecting a given amount of liquid (hydrocarbons); As a result of optimal contacting of the hydrocarbon feed and catalyst particles 10, the formation of coke deposits on the catalyst particles and on the walls of the cracking device is reduced.
    权利要求:
    Claims (4)
    [1]
    Invention Formula
    15 1. A device for contacting solid crushed particles with a liquid, comprising a housing, fluid supply pipes, mounted concentrically along the axis of the housing with a gap
    20 relative to each other, a pipe for supplying liquid in the lower part of the housing and a pipe for feeding solid particles and a reflector, characterized in that
    25 to increase the efficiency of the process; it is provided with a boundary pipe with a distribution device installed coaxially with the liquid supply pipes, while the internal pipe
    30 is made with a tapered upper part, and the ratio of the diameters of the lower part to the upper part is 1-5,
    [2]
    2. A device according to claim 1, characterized in that the reflector is made in the form of a cone with an opening angle of 80-120 °, which faces its tip towards the outlet of the constricted part of the pipe for supplying liquid.
    [3]
    3. The device according to paragraphs. 1 and 2, characterized in that the distribution device is in the form of a grid.
    [4]
    4. Device on PP. 1-3, characterized in that the switchgear is made in video
    five
    de ring bubbler,
    haassesari
    Fiz1
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1551240A3|1990-03-15|Apparatus for contacting solid pulverized particles with liquid
    RU2002108352A|2003-11-10|INITIAL MATERIAL INJECTION SYSTEM FOR CATALYTIC CRACKING PROCESS
    RU2070441C1|1996-12-20|Device for separation of solid particles from mixture of solid substances and liquid or gaseous medium
    CA2303307C|2005-08-02|Throat and cone gas injector and gas distribution grid for slurry reactor
    JP3157189B2|2001-04-16|Apparatus and method for introducing catalyst particles into a moving bed of catalyst, and apparatus for catalytic cracking of hydrocarbonaceous feedstock
    US4289729A|1981-09-15|Biased degasser for fluidized bed outlet
    US2798030A|1957-07-02|Method and device for injecting a fluid into a fluidized bed of a particulate material
    EP0239171B1|1993-02-24|Apparatus and process for mixing fluids
    SU786864A3|1980-12-07|Device for separating fluidized flow to several secondary flows
    US3607126A|1971-09-21|Flow-directing device
    US3848811A|1974-11-19|Device for injecting a fluid into a fluidized bed of particulate material
    JPH0712470A|1995-01-17|Method and device for distribution of fluid to container
    US3607127A|1971-09-21|Apparatus for conversion of hydrocarbons
    US4824557A|1989-04-25|Process for mixing cracking catalyst with a fluid hydrocarbon
    US5552119A|1996-09-03|Method and apparatus for contacting solid particles and fluid
    US4675099A|1987-06-23|Flowing catalyst particles in annular stream around a plug in lift pot
    US20030027876A1|2003-02-06|Throat and cone gas injector and gas distribution grid for slurry reactor |
    US2652317A|1953-09-15|Reactor inlet
    US4808382A|1989-02-28|Process for mixing cracking catalyst with a fluid hydrocarbon
    US4711766A|1987-12-08|Apparatus for mixing cracking catalyst with a fluid hydrocarbon
    US4624836A|1986-11-25|Apparatus and process for mixing cracking catalyst with a fluid hydrocarbon
    US6486217B2|2002-11-26|Throat and cone gas injector and gas distribution grid for slurry reactor |
    US2999012A|1961-09-05|Apparatus for contacting hydrocarbons with solids
    CA1314259C|1993-03-09|Liquid degaser in an ebullated bed process
    SU1033175A1|1983-08-07|Apparatus for carrying out processes in fluidized bed
    同族专利:
    公开号 | 公开日
    ES2019090B3|1991-06-01|
    EP0241966B1|1990-11-07|
    NL8700705A|1987-10-16|
    AU594138B2|1990-03-01|
    AT58159T|1990-11-15|
    CN1017972B|1992-08-26|
    CN87102269A|1987-11-25|
    AR242916A1|1993-06-30|
    DE3765977D1|1990-12-13|
    EP0241966A1|1987-10-21|
    AU7063187A|1987-10-01|
    IN169344B|1991-09-28|
    CA1288931C|1991-09-17|
    GB8607698D0|1986-04-30|
    SG28592G|1992-06-12|
    MX170622B|1993-08-31|
    JPS62237940A|1987-10-17|
    MY102297A|1992-05-28|
    US4795547A|1989-01-03|
    BR8701392A|1988-01-05|
    ZA872187B|1987-09-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2948671A|1955-11-14|1960-08-09|Exxon Research Engineering Co|Fluid hydroformer reactor distributor|
    US3071540A|1959-10-27|1963-01-01|Kellogg M W Co|Oil feed system for fluid catalytic cracking unit|
    US3152065A|1961-09-14|1964-10-06|Exxon Research Engineering Co|Feed injector for cracking of petroleum|
    US3848811A|1973-12-19|1974-11-19|Sun Oil Co Pennsylvania|Device for injecting a fluid into a fluidized bed of particulate material|
    US4391611A|1981-03-05|1983-07-05|The United States Of America As Represented By The United States Department Of Energy|Gasification system|
    US4414101A|1981-08-17|1983-11-08|Standard Oil Company |Hydrocarbon conversion method and apparatus|
    US4427537A|1982-03-17|1984-01-24|Dean Robert R|Method and means for preparing and dispersing atomed hydrocarbon with fluid catalyst particles in a reactor zone|
    IT1168698B|1983-11-21|1987-05-20|Finike Italiana Marposs|HEAD FOR THE CONTROL OF LINEAR DIMENSIONS|
    US4563334A|1983-12-02|1986-01-07|Phillips Petroleum Company|Catalytic cracking unit|
    US4555328A|1984-01-19|1985-11-26|Mobil Oil Corporation|Method and apparatus for injecting liquid hydrocarbon feed and steam into a catalytic cracking zone|
    EP0180291A1|1984-10-26|1986-05-07|Mobil Oil Corporation|Feed mixing technique for fluidized catalytic cracking of hydrocarbon oil|
    US4687642A|1985-01-08|1987-08-18|Phillips Petroleum Company|Fluid feed apparatus|US4957617A|1986-09-03|1990-09-18|Mobil Oil Corporation|Fluid catalytic cracking|
    US5160706A|1989-10-17|1992-11-03|Shell Oil Company|Process for the catalytic cracking of a hydrocarbon oil|
    EP0593171B1|1992-10-13|1996-09-11|Abb Lummus Global Inc.|Method for atomizing feedstock in a fluid catalytic cracking process|
    CH689284A5|1995-02-16|1999-01-29|Buehler Ag|Shaft reactor with descending bed of granular material, for post|
    US6387247B1|1999-09-03|2002-05-14|Shell Oil Company|Feed injection system for catalytic cracking process|
    DE10260739B3|2002-12-23|2004-09-16|Outokumpu Oy|Process and plant for producing metal oxide from metal compounds|
    DE10260731B4|2002-12-23|2005-04-14|Outokumpu Oyj|Process and plant for the heat treatment of iron oxide-containing solids|
    DE10260738A1|2002-12-23|2004-07-15|Outokumpu Oyj|Process and plant for conveying fine-grained solids|
    DE10260733B4|2002-12-23|2010-08-12|Outokumpu Oyj|Process and plant for the heat treatment of iron oxide-containing solids|
    DE10260734B4|2002-12-23|2005-05-04|Outokumpu Oyj|Process and plant for the production of carbon coke|
    DE10260741A1|2002-12-23|2004-07-08|Outokumpu Oyj|Process and plant for the heat treatment of fine-grained solids|
    DE10260737B4|2002-12-23|2005-06-30|Outokumpu Oyj|Process and plant for the heat treatment of titanium-containing solids|
    DE102004042430A1|2004-08-31|2006-03-16|Outokumpu Oyj|Fluidized bed reactor for the thermal treatment of vortex substances in a microwave-heated fluidized bed|
    EP2045002A1|2007-10-02|2009-04-08|Ineos Europe Limited|Mixing apparatus|
    WO2011080754A2|2009-12-29|2011-07-07|Indian Oil Corporation Ltd.|A feed nozzle assembly|
    WO2014064109A1|2012-10-25|2014-05-01|Shell Internationale Research Maatschappij B.V.|Feed nozzle assembly for a catalytic cracking reactor|
    CN103394311B|2013-08-08|2015-07-01|攀钢集团攀枝花钢铁研究院有限公司|Device and process for liquid-solid fluidized reaction|
    CN109382046B|2017-08-11|2021-03-09|中国石油天然气股份有限公司|Fixed fluidized bed reactor feeding system|
    CN110961268A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Atomizing nozzle for lifting pipe|
    CN110961049A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Riser catalytic cracking unit|
    CN110961048A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Atomizing nozzle for catalytic cracking device|
    CN110961043A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Riser catalytic cracking unit|
    CN110961051A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Atomizing nozzle for catalytic cracking unit reaction|
    CN110961045A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Riser catalytic cracking unit|
    CN110961052A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Riser catalytic cracking unit|
    CN110961047A|2018-09-30|2020-04-07|中国石油天然气股份有限公司|Nozzle for catalytic cracking device|
    WO2021018828A1|2019-07-30|2021-02-04|Shell Internationale Research Maatschappij B.V.|Riser reactor system|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB868607698A|GB8607698D0|1986-03-27|1986-03-27|Contacting particulate solids with fluid|
    [返回顶部]