• 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:
    Regeneration of a spent hydrocarbon conversion catalyst is accomplished by means of a moving bed of catalyst, where catalyst is passed through several treatment zones, in a unique regeneration vessel. The catalyst is first contacted with a hot oxygen-containing gas stream in a burning zone in order to remove coke. The catalyst is then passed into a drying zone for removal of water formed in the combustion zone by passing a hot dry air stream through the catalyst. This hot air stream is produced by exchange of heat with catalyst, thereby effecting cooling of the regenerated catalyst and by use of an air heating means located in the vessel. After passing through the drying zone, the air stream provides oxygen for combustion in the combustion zone.
    公开号:SU1577686A3
    申请号:SU864028768
    申请日:1986-12-26
    公开日:1990-07-07
    发明作者:Раймонд Гринвуд Артур
    申请人:Юоп Инк (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the catalytic conversion of hydrocarbons into useful hydrocarbon products, more specifically to the regeneration of spent catalyst.
    The aim of the invention is to intensify the process of regeneration of spent catalyst particles.
    FIG. 1 shows the proposed device, a longitudinal vertical section; in fig. 2 is a section A-A in FIG. in fig. 3 is a section BB in FIG. one,
    The device contains a regenerative capacity of 1 variable cross section, in the upper part of which a larger diameter is located combustion chamber 2 and the halogenation chamber 4 separated from it by a transverse partition 3, and a catalyst drying and cooling chamber 5 located in the lower part of a smaller diameter. In the combustion chamber 2 and the halogenation chamber 4 there are two concentrically mounted perforated screens 6 and 7 for holding the catalyst, forming between them a channel 8 for the passage of the catalyst. The channel 8 in the lower part is open and communicates with the drying zone of the lower chamber 5. The outer perforated screen 7 forms with the wall of the upper chamber 2 a channel 9 for distributing the gas to which the pipe 10 for supplying the regenerating gas and the pipe 11 for the supply of halogen are connected. The nozzle 12, the lower end of which is located in the upper part of the annular channel, is connected to the nozzle 13 for supplying the spent catalyst. Pipe 14 for air intake with pris
    -four
    00
    The air distribution method 15 is located in the cooling zone of the lower chamber 5. The halogen exhaust nozzle 16 is connected to the halogen inlet nozzle through a nozzle 17 located along the axis of the inner shield 6. Above the distributor is located the heating device 18.
    The device works as follows.
    Catalyst particles are introduced into the regeneration tank 1 by means of nozzles 12. Although FIG. Figure 1 shows two inlet ports 12 for a catalyst; only one port or several nozzles can be used. The two screens 6 and 7 for holding the catalyst are located inside the upper part of the regeneration tank 1, have a cylindrical shape, and their central axis is the central axis of the regeneration tank, while they are arranged in a concentric manner in the upper part of the regeneration tank. The screens 6 and 7 form an annular channel 8 through which the catalyst bed moves under the influence of gravity. The catalyst inlets 13, which are a continuation of the nozzles 12, provide a supply of the catalyst to points that are spatially separated from each other around the annular layer. Catalyst screens have holes that are small enough to prevent catalyst particles from passing through screens or to get stuck in this screen; The screens for holding the catalyst pass through the upper part of the tank 1 and provide the supply of the catalyst to the drying zone of the lower chamber 5.
    An annular channel 9, which is used to distribute the gas around the catalyst, is formed between the screen 7 for holding the catalyst and the side wall of the upper part of the regeneration tank 1. The gas enters this channel, which ensures its distribution by means of the recycle pipe 10 that has an annular shape a barrier between channel 9 for gas distribution and a similar annular channel 19 for gas distribution, which is a continuation of channel 9. Gas flows in a radial direction enii through the catalyst., held between screens 6 and 7, having a central cylindrical passage 20, part of which occupies 17 pipe for halogen.
    The part of the upper part of the tank 1, which is located above the partition 3, is the combustion chamber 2, where coke burns. The part of the upper part of the vessel that passes under the partition 3 is a halogenation chamber 4. In some applications, there is no need to create a halogenation chamber, in which case the partition 3, branch pipe 17, inlet port 11 for halogen and outlet port 16 can be excluded. The gas containing halogen enters the zone through port 11 and passes through the catalyst in the radial direction, while entering into the central space of the inner screen 6 of the halogenation chamber 4.
    Screens 6 and 7 extend to the lower part of the vessel, which has a smaller diameter than the upper part. The outer diameter of the screen 7 is slightly smaller than the inner diameter of the lower chamber, and the screens protrude inward the lower part to ensure sealing, so that virtually all the gas contained in the annular distribution channel 19 flows through the catalyst instead of bypassing it. by passing to the bottom of the regeneration tank. Other sealing means may be used. The catalyst discharged from the annular channel between the screens for holding the catalyst fills the entire bottom of tank 1 with the exception of the space below the screen for catalyst 21 that contains heating means 18. The catalyst moves down through the bottom of the tank and out of the container through the exit nozzle 22 catalyst. It passes from the annular layer and through the drying zone, the heating zone and the cooling zone of the catalyst.
    The nozzle 14 on the regeneration tank 1 is provided with means 15 for distributing air to various points in the horizontal plane, which is located perpendicular to the descending catalyst so that it flows evenly up the column in contact with the entire mass of the catalyst. Soo
    The air entering the vessel has a temperature of about 38 ° C. The air passes upward through the catalyst in the lower portion of the tank (catalyst cooling zone), then is heated by the catalyst in the cooling zone to a temperature of approximately 482 ° C. In turn, the catalyst is cooled to a temperature of from 149 to 204 ° C. The air is then heated by the heating means 18 installed above.
    The heating means 18 can be made in the form of tubes 23 containing a heat-giving liquid, however, preferably they correspond to electrical resistance heating elements. The heating pipes 23 are connected to the leveling means 24 of the heating device 18. The catalyst passes by the heating means through the catalyst passage defined by the plates 25 and 26 and the side wall of the lower part of the tank 1. The upper part of the space occupied by the heating means is covered with a screen 21 for in order to eliminate the possibility of catalyst particles entering this space. In fact, all the air passes through the heating means instead of passing up through the catalyst in the passages, since the pressure drop of air flowing upward into these passages going down is much greater than the pressure of air flowing upward through the heating means. Average value
    five
    0
    the mass of air enters the pipe 17. This is accomplished by providing means 27 for directing the flow, such as, for example, an expanded end of the pipe 17. The gas containing halogen that passed through the catalyst also enters the pipe 17.
    The halogen nozzle 17 is centrally located relative to the vertical axis of the container. The screens 6 and 7 for holding the catalyst limit the downstream channel 8 for the catalyst. The gas in channel 9 for distribution flows radially through the pipe; catalyst in central space - 28, which is determined by the screen b and the pipe 17.
    The part of the halogen-containing gas g, which enters through the nozzle 11 for halogen, passes through the catalyst junction and immediately enters the central space 28, 5 This deviation of the gas is carried out using means 27 to direct the flow. It is this part of the gas that provides oxygen for combustion.
    The gas escaping from the vessel through the 0 outlet 16 is compressed and the recirculation is fed into the regeneration tank with the inlet 11 for the gene. Chlorine and steam are added to the recycled gas and heated before being returned to the tank. Truth of all, this gas can be air, since it contains virtually all the air flowing upwards from the side of the tank. Gas entering the spine
    five
    the temperature of the ascending air & Q through the nozzle 11, directed into the zoduh after passing it through the heating zone, is approximately 538PC.
    The heated air passes upward through the catalyst, which is located in that part of the tank, which is designated as a drying zone, leaving in it moisture that was contained in the catalyst. In fact, all the air moving up the column from the drying zone 18 passes inside the central space of a cylindrical shape, limited by a screen 6 for holding the catalyst. The main part of the air then enters the halogen nozzle 17 in order to exit the regeneration tank through the halogen nozzle 16. In most cases, the container is designed in such a way that virtually all
    five
    WITH
    five
    by halogenating with partition 3. The gas containing halogen is distributed through the annular channel 19 and passes radially through a portion of the catalyst bed laid below the partition 3, thus providing a halogenated catalyst. Pass the catalyst, the oil is mixed with the upward air in the central space and then enter the halogen nozzle 17. The recirculated gas enters the annular channel 9 for the gas propellant by means of the nozzle 10 and passes radially through the catalyst bed of particles and into the annular central space 28 The gas passing through the catalyst in the combustion zone provides KMS
    for combustion of carbon on the catalyst in the combustion zone, and then mixed with a part of the rising gas from the halogenation zone, which does not enter the pipe 17, and the mixture (exhaust gases) flows out of the vessel through the pipe 29. A part of the gas is emitted into the atmosphere through a scrubber, if necessary, and the remainder is compressed under pressure and returned to the vessel through nozzle 10. If necessary, for example, to remove sulfur oxides, the recirculated gas is cleaned before it is returned to the tank. l 1 through pipe 10.
    权利要求:
    Claims (2)
    [1]
    1. A device for the regeneration of spent catalyst particles used in hydrocarbon conversion reactions, comprising a vertical housing, comprising combustion and halogenation chambers located in the upper 25 of a large diameter, separated by a transverse partition, and a drying zone in the lower part of a smaller diameter and cooling, 30 two cylindrical vertical-spaced vertical perforated screens to hold the catalyst to form a passage between them pa $ communication with the drying zone of the lower chamber, and koltseQ 5
    0
    5 30 $
    channel between the wall of the upper chamber and the outer screen for gas distribution, fitting for introducing spent catalyst with a pipe, the lower end of which is located in the upper part of the annular channel for the passage of the catalyst, pipe for supplying regenerating gas connected to the ring channel for gas distribution, pipe for supplying flue gases, communicating with the central space of the inner screen, air inlet fitting with air distribution device located in the cooling zone the lower chamber, a halogen inlet connection that communicates with the halogenation zone and the halogen outlet connection through a pipeline located along the axis of the inner screen, characterized in that, in order to intensify the regeneration process, it is equipped with a means of heating the air located along the axis in the lower chamber above the fixture for distributing the air under the drying zone to form an annular intake with the chamber walls for the passage of the catalyst.
    [2]
    2. A device according to claim 1, characterized in that the means for heating the air are made in the form of a stack of pipes arranged between vertical plates and a gas permeable screen located above it.
    15
     / - :. :.
    : -:;:. .V -, -
    №К /
    25
    FIG.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1577686A3|1990-07-07|Device for regeneration of used particles of catalyst
    US3652231A|1972-03-28|Reconditioning system for moving column of reforming catalyst
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    US4147523A|1979-04-03|Apparatus for continuously treating gas with activated carbon
    KR101682734B1|2016-12-05|Utilization of baffles in chlorination zone for continuous catalyst regeneration
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    US5407647A|1995-04-18|Gas-scrubber apparatus for the chemical conversion of toxic gaseous compounds into non-hazardous inert solids
    US3378349A|1968-04-16|Apparatus for treating mixed-phase fluid reactants
    US2525925A|1950-10-17|Process utilizing solid carrier particles
    US5069169A|1991-12-03|Tube-in-shell heating apparatus
    GB1495291A|1977-12-14|Device for treating gases
    US4832921A|1989-05-23|Apparatus for regeneration of hydrocarbon conversion catalyst
    US5397381A|1995-03-14|Method of cooling and optionally cleaning a hot gas, especially of a gas generated upon combustion or gasification of carbon-containing fuels
    JPH0924268A|1997-01-28|Reaction column
    US2436780A|1948-02-24|Method for handling a contact mass
    US2391315A|1945-12-18|Reactor
    US3806324A|1974-04-23|Air distribution system for catalyst regenerator
    US2475822A|1949-07-12|Catalytic reaction apparatus
    US2458358A|1949-01-04|Process of regenerating a moving bed of solid catalyst
    US4207292A|1980-06-10|System for reducing sulfur dioxide
    RU2107540C1|1998-03-27|Apparatus for conduction of catalytic reaction in fluidized bed
    US3192905A|1965-07-06|Combined carbon monoxide oxidizer and fluid heater
    US2458356A|1949-01-04|Method and apparatus for burning contaminants from a moving bed contact mass
    US2566285A|1951-08-28|Method for regeneration of moving catalysts
    US9868118B2|2018-01-16|Process for regenerating catalyst particles
    同族专利:
    公开号 | 公开日
    NO865249D0|1986-12-22|
    JPS62191038A|1987-08-21|
    US4647549A|1987-03-03|
    MY101859A|1992-01-31|
    CA1270783A|1990-06-26|
    AT61254T|1991-03-15|
    NO865249L|1987-06-29|
    GR3001572T3|1992-11-23|
    CN86108969A|1987-07-29|
    ES2021276B3|1991-11-01|
    AU581113B2|1989-02-09|
    KR870005692A|1987-07-06|
    EP0227080A2|1987-07-01|
    EP0227080B1|1991-03-06|
    EP0227080A3|1988-04-20|
    DE3677919D1|1991-04-11|
    CN1003914B|1989-04-19|
    KR900000752B1|1990-02-15|
    AU6653586A|1987-07-02|
    NO169424B|1992-03-16|
    NO169424C|1992-06-24|
    IN169259B|1991-09-21|
    NZ218643A|1988-08-30|
    ZA869479B|1988-04-27|
    JPH055536B2|1993-01-22|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2833726A|1952-12-03|1958-05-06|Socony Mobil Oil Co Inc|Method and apparatus for cooling granular contact material|
    US3647680A|1969-09-25|1972-03-07|Universal Oil Prod Co|Continuous reforming-regeneration process|
    US3652231A|1969-09-25|1972-03-28|Universal Oil Prod Co|Reconditioning system for moving column of reforming catalyst|
    US3692496A|1971-04-19|1972-09-19|Universal Oil Prod Co|Apparatus for continuous reforming-regeneration process|
    US3745112A|1971-11-23|1973-07-10|Universal Oil Prod Co|Platinum-tin uniformly dispersed hydro-carbon conversion catalyst and process|
    US3838038A|1971-12-14|1974-09-24|Universal Oil Prod Co|Continuous conversion and regeneration process|
    US3978150A|1975-03-03|1976-08-31|Universal Oil Products Company|Continuous paraffin dehydrogenation process|
    US4094817A|1977-06-15|1978-06-13|Uop Inc.|Regeneration method for gravity-flowing deactivated catalyst particles|
    US4094814A|1977-06-15|1978-06-13|Uop Inc.|Regeneration method for gravity-flowing deactivated catalyst particles|
    US4438288A|1983-03-22|1984-03-20|Uop Inc.|Dehydrogenation of hydrocarbons with a halogen contacting step|
    US4506032A|1983-03-22|1985-03-19|Uop Inc.|Dehydrogenation catalyst composition|US4859643A|1988-05-11|1989-08-22|Uop|Regeneration method with reduced catalyst heat exposure|
    JPH02298356A|1989-05-09|1990-12-10|Sofutaade Kogyo Kk|Method and apparatus for regenerating catalyst|
    US5227566A|1991-01-09|1993-07-13|Uop|Process for the dehydrogenation of hydrocarbons|
    US5087792A|1991-01-09|1992-02-11|Uop|Process for the dehydrogenation of hydrocarbons|
    US5824619A|1994-05-12|1998-10-20|Uop|Particulate cooling process with reduced thermal channeling|
    NZ304308A|1995-03-20|1998-02-26|Shell Int Research|Regeneration of catalyst particles contaminated with carbonaceous and/or sulphur containing materials|
    CN1089639C|1998-07-10|2002-08-28|中国石油化工集团公司|Regeneration method of hydrocarbon converting catalyst|
    US6123833A|1998-09-22|2000-09-26|Uop Llc|Method for controlling moisture in a catalyst regeneration process|
    CN1089640C|1999-05-19|2002-08-28|中国石油化工集团公司|Regeneration process of hydrocarbon converting catalyst|
    CN1089641C|1999-05-19|2002-08-28|中国石油化工集团公司|Regeneration process of hydrocarbon converting catalyst|
    US7282619B2|2003-10-14|2007-10-16|Shell Oil Company|Method of operating a dehydrogenation reactor system|
    US8262773B2|2005-07-26|2012-09-11|Exxonmobil Upstream Research Company|Method of purifying hydrocarbons and regeneration of adsorbents used therein|
    FR2934963B1|2008-08-13|2010-11-26|Inst Francais Du Petrole|CATALYST REGENERATION APPARATUS AND ASSOCIATED REGENERATION METHOD|
    FR2957821B1|2010-03-24|2014-08-29|Inst Francais Du Petrole|NEW AREA OF CATALYST REGENERATION DIVIDED IN SECTORS FOR REGENERATIVE CATALYTIC UNITS|
    US20150224464A1|2014-02-13|2015-08-13|Uop Llc|Radial flow reactor having a side inlet nozzle and methods for reacting hydrocarbons using the same|
    法律状态:
    2007-09-20| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: MM4A Effective date: 20041227 |
    优先权:
    申请号 | 申请日 | 专利标题
    US06/814,337|US4647549A|1985-12-27|1985-12-27|Regeneration of hydrocarbon conversion catalyst|
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