• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
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  • 优先权
    • 专利摘要:
    1408007 Discharging catalyst UNIVERSAL OIL PRODUCTS CO 17 Nov 1972 [18 Nov 1971] 53138/72 Heading B1F Catalyst is withdrawn from moving catalyst bed (17), (Fig. 2, not shown) in relatively equal amounts through uniformly distributed outlets (21), where it contacts a countercurrent hydrogen stream, to chambers 41, Fig. 6, of relatively equal volume formed by radial vertical partitions 25, the flow of catalyst to each chamber 41 automatically stopping when the level in the chamber reaches the discharge point of the respective conduits 22. The flow of catalyst through outlets 21 is stopped e.g. by increasing the upward flow of hydrogen through conduits 22 when catalyst is discharged from chambers 41 through the bottom outlet of collector 23. The catalyst can be withdrawn from the beds 17 while the reactor containing them is maintained in an onstream condition for reforming hydrocarbons.
    公开号:SU735157A3
    申请号:SU721851052
    申请日:1972-11-17
    公开日:1980-05-15
    发明作者:Мильтон Бойд Дэвид；Раймонд Гринвуд Артур
    申请人:Юниверсал Ойл Продактс Компани (Фирма)；
    IPC主号:
    专利说明:

    (54) APPARATUS WITH MOVING CATALYST LAYER
    one
    The invention relates to apparatus with a moving catalyst bed and can be used in the petrochemical industry, for example, in unreformed reforming processes .5
    Apparatus are known in which the entire mass of a catalyst is periodically or uninterruptedly moved by gravity. These devices are equipped with devices that provide a certain degree of uniformly-JQ overload of catalyst 1. When carrying out the conversion reaction of hydrocarbons in a moving bed reactor, it is necessary that the residence time of the catalyst in the reactor is kept constant. In the case of ecmi, there are significant time deviations of pre-catalyst, then the catalyst remaining in the reactor longer than necessary can agglomerate due to the formation of carbonaceous deposits, resulting in a subsequent deterioration of the distribution in the catalyst stream.
    Closest to the invention is an apparatus with a moving bed of catalyst.
    including a catalyst chamber with a bottom and a reservoir located under it for unloading the catalyst, containing pipes, the upper ends of which are fixed in the bottom of the catalyst chamber, and the lower ones are placed at one common height in collection 2.
    This apparatus removes the catalyst and a plurality of points evenly spaced around the cross-sectional area of the chamber.
    The disadvantages of the known apparatus are uneven overload rates along the pipes and undesirable deviations during the residence time of the catalyst.
    The aim of the invention is to improve the catalyst overload uniformity.
    The goal is achieved by the fact that the collector is provided with partitions vertically installed between the pipes, dividing the assembly by the number of pipes into equal sections communicating with each other in the upper and lower parts of the assembly. ,
    FIG. I shows the proposed apparatus with a moving catalyst bed and a assembled assembly; in fig. 2 - catalyst chamber of apgarata is shown; in fig. 3 - the AA section in FIG. one; in fig. 4 - one of the reloading tubes, built into the bottom of the catalyst chamber; ka fig. 5 is a section along BB in FIG. G; in fig. 6 - arrangement of pipes and partitions in the collection; in fig. 7 - option to complete the collection. The device 1, which was made adjacent to the race naphtha reforming process, contains chambers 2 and 3 with a catalyst, a 4-day catalyst collection, overheat pipelines 5, the lower ends of which are located at one common height in the collection, and the upper ones are fixed in the bottom 6 of the catalyst chamber 3. Collection 4 is provided with a partition wall 7 dividing it into paBHbie sections 8 communicating with each other in the upper 9 and lower 10 parts of the collection. The device works in a manner that follows. The direct-run naphthage fraction (equal to 93-204 0) flows through conduit II, mixes with the flow of hydrogen-enriched gas recycle, nocjy strikes lean through conduit 12 and enters the heater 14 through 1J in the heater. The heated mixture enters the apparatus through line 15. . The catalyst is fed through conduit 16 to section 17 to recover the catalyst n and then, via nozzles 18, to the upper ejection chamber of the ashyrate. Under the action of gravitational forces, the catalyst passes through cattle-catcher chambers 2 and 3 and through pipelines 5 to overflow to collector 4, divided into sections according to the number of pipelines by vertical partitions 7 The catalyst flows through the reloading pipeline until its level reaches the lower end of the pipeline. In that
    权利要求:
    Claims (2)
    [1]
    735157, the flow of catalyst in the pipeline stops automatically. Since the catalyst cannot cross between sections because of the presence of partitions, the total volume of the catalyst taken from each point of the catalyst chamber remains constant until the collection is full. Then sborgshk unload into the bunker 19, stopping the flow of catalyst in pipelines 5 gas supply through the pipeline 20. Unloaded catalyst is returned to the apparatus by pneumatic transport, zab} fa it from the lifting bunker 21., Apparatus of the invention with a moving bed of catalyst, including a catalyst chamber with a bottom and a collector disposed below therein for discharging a catalyst containing tubes, the upper ends of which are the ucregtep, are in the bottom of the catalyst chamber, and the lower ones are placed at one common height in the collector, characterized in that In order to improve the catalyst overload uniformity, the collector is equipped with partitions vertically installed between the pipes, dividing .je6opmnc by the number of pipes into equal sections communicating with each other in the upper and lower parts of the collector. Sources of information taken into account in the examination 1. US patent number 3470090, cl. 23-258, 1972.
    [2]
    2. J. Perry. Handbook of chemical engineer, translation from English, 1969, p. 269.
    .four
    类似技术:
    公开号 | 公开日 | 专利标题
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    US2606863A|1952-08-12|Process and apparatus for the conversion of hydrocarbons and the stripping of vaporizable hydrocarbons from the fouled catalyst
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    US3198729A|1965-08-03|Continuous conversion of hydrocarbons with sensitive catalyst
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    US2695815A|1954-11-30|Method of and apparatus for pneumatic transfer of granular contact material in moving bed hydrocarbon conversion processes
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    US2745724A|1956-05-15|Disengagement of gases from a moving bed of fluent solid particles
    US2935461A|1960-05-03|Catalytic cracking of heavy charge stocks
    US2715048A|1955-08-09|Method and apparatus for elevating granular material
    同族专利:
    公开号 | 公开日
    IE36843L|1973-05-18|
    FR2160432B1|1977-08-26|
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    AR200719A1|1974-12-13|
    IE36843B1|1977-03-02|
    JPS4862673A|1973-09-01|
    DE2255408B2|1975-09-11|
    DK142485B|1980-11-10|
    DE2255408A1|1973-05-30|
    NL7215502A|1973-05-22|
    NO132675B|1975-09-08|
    JPS5543380B2|1980-11-06|
    DD105249A5|1974-04-12|
    ES408700A1|1976-03-01|
    ZA727920B|1973-07-25|
    MY7600257A|1976-12-31|
    US3785963A|1974-01-15|
    DK142485C|1981-07-06|
    AU471231B2|1976-04-15|
    AU4864572A|1974-05-09|
    SE381993B|1976-01-12|
    AT323869B|1975-08-11|
    GB1408007A|1975-10-01|
    PL85025B1|1976-04-30|
    NL173144C|1983-12-16|
    BG26818A3|1979-06-12|
    NO132675C|1975-12-17|
    IT974834B|1974-07-10|
    BR7208064D0|1973-08-23|
    EG10903A|1976-08-31|
    FR2160432A1|1973-06-29|
    NL173144B|1983-07-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3856662A|1973-04-02|1974-12-24|Universal Oil Prod Co|Method for solids-withdrawal and transport from a superatmospheric pressure system|
    US3873441A|1973-09-06|1975-03-25|Universal Oil Prod Co|Catalyst transfer method for moving-bed reactors|
    US3978150A|1975-03-03|1976-08-31|Universal Oil Products Company|Continuous paraffin dehydrogenation process|
    US4110081A|1977-06-09|1978-08-29|Uop Inc.|Moving-bed radial flow solids-fluid contacting apparatus|
    FR2434648B1|1978-08-30|1981-02-27|Uop Inc|
    FR2460990B1|1979-07-09|1984-01-13|Inst Francais Du Petrole|
    US4403909A|1980-03-24|1983-09-13|Uop Inc.|Method for discharging catalyst particles from a moving bed system at a substantially steady flow rate|
    US4478793A|1982-09-22|1984-10-23|Uop Inc.|Radial flow reactor with operating temperature profile|
    US4968409A|1984-03-21|1990-11-06|Chevron Research Company|Hydrocarbon processing of gas containing feed in a countercurrent moving catalyst bed|
    EP0403475B1|1988-01-29|1993-11-10|THACKER, Milton B.|Low profile fluid catalytic cracking apparatus and method|
    US4925632A|1988-01-29|1990-05-15|Thacker Milton B|Low profile fluid catalytic cracking apparatus|
    US5516422A|1994-05-06|1996-05-14|Uop|Interreactor particle transfer process and arrangement|
    JP2002273199A|2001-03-15|2002-09-24|Idemitsu Petrochem Co Ltd|Method for drawing out gaseous fluid|
    US9006123B2|2008-12-23|2015-04-14|Uop Llc|Catalytic reformer catalyst collector including purge gas stream|
    CN107429171A|2015-03-31|2017-12-01|环球油品公司|Method and apparatus for integrating isomerization and platforming technical process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US20012371A| true| 1971-11-18|1971-11-18|
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