• 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:
    A system is disclosed for circulating an ancillary hydrogen-rich gas stream through a part of a moving bed hydrocarbon conversion process. The gas stream may be employed in lockhopper systems, catalyst transfer equipment and catalyst treating zones as for reducing the catalyst. The used ancillary gas is discharged into a partitioned vapor-liquid separation vessel. The partially condensed reaction zone effluent stream is discharged into a different chamber of the same vessel. The net off gas stream is withdrawn from the chamber receiving the used ancillary gas to prevent contamination of a recycle gas stream, which is drawn off the other chamber.
    公开号:SU1713421A3
    申请号:SU864027094
    申请日:1986-01-27
    公开日:1992-02-15
    发明作者:Раймонд Гринвуд Артур
    申请人:Юоп Инк. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to an apparatus with a moving catalyst bed and can be used to carry out various methods for the catalytic conversion of hydrocarbons, such as: reforming, hydrotreating, dehydrogenation and dehydrocyclomerization, as well as regeneration of a coke-contaminated catalyst.
    The aim of the invention is to intensify the process of regeneration of the catalyst.
    FIG. 1 shows the apparatus, a longitudinal section; in fig. 2 - the same, part of the longitudinal section; in fig. 3 is a section on A-A in FIG. 2
    The apparatus containing the two-stage regenerator section includes a vertical pressure reservoir 1. The removable cover 2 is connected to the cylindrical outer wall of the reservoir. The non-perforated end ring element 3 is welded by its upper end to the cover 2, and by its lower end to the upper
    the end of the perforated inner mesh cylinder 4. Through the lid 2 passes a large number of inlet pipes 5, designed to receive the used catalyst from a reactor or other source. In addition, an exhaust fitting 6 is installed on the lid. It is designed to remove gases from the reservoir. The radial support flange 7 of the sieve is installed between flanges 8 and 9 on the cover 2 and wall 1 and serves to mount a perforated outer mesh cylinder 10 having an upper mounting ring portion 11 that hangs down. The annular cavity between the inner and outer mesh cylinders 4 and 10 forms a top processing zone 12 containing a column of 13 of the used catalyst particles with deposits of coke on them. There is usually coke so that the carbon content is 5% by weight of the catalyst particles . Zone 12 may be referred to as the carbon burn zone, since coke is usually removed or burned when the particles are continuously in contact with the flow of the first treatment gas entering zone 12 through the gas-vapor inlet means 14 and the annular distribution section 15 between wall 1 and the grid cylinder 10. The preferred first gas is recirculated flue gas, e.g. gas exiting through outlet fitting 6, to which sufficient air is added to obtain a relatively low oxygen content, like Example 0,8%. The low oxygen content inhibits the burning rate of carbon, controlling the maximum temperature to which the catalyst particles are exposed, and thus protecting them from overheating. The ability of the plant to provide accurate sample testing can allow for the regulation of the oxygen level in the first gas in order to reduce the temperature and increase the service life of the catalyst.
    Immediately after the upper zone is followed by a transit zone 16, having at its upper end an inner non-perforated ring element 17 welded to the lower end of the mesh cylinder 4 and a similar end ring element 18 welded to the outer perforated mesh cylinder TO. The lower end of the transit zone 16 on its inner surface is formed by a cylindrical inner wall of the transit element 17.
    As shown in FIG. 2, the transit zone has a downwardly conical shape in cross section, since its outer wall is formed by an angled conical part 19 and a vertical part 20. Thus, in its upper part, the transit zone has a width equal to the width d of the radial gap between the sieves 4 and 10, while at its base it has a width d, which is preferably less than 50% d. Although the transit zone 16 may have parallel side walls and an annular cross-section of constant width, however, the conical structure for a given height h of the transit zone results in a decrease in the amount of first gas that can pass down through the transit zone width d. This decrease in flow is due to the increase in back pressure created by particles in the catalyst bed when they must pass through a confined orifice. The presence of a conical shape in the cross section of the transit zone 16 also causes an increase in the velocity of the particles in the column 13 as they pass through the transit zone downwards. The downward movement of the particles is aided by the fact that a small part of the gas in the upper gas processing zone 12 will move downward, as shown by the current lines in FIG. 2
    Obviously, particles that have completed their downward movement through the upper processing zone 12 and passed into the transit zone 16 will truly represent the degree of coke burnout achieved in zone 12. This condition will be met, since the particles do not have the possibility of contact with gas, relatively richer oxygen coming in through inlet 21 and upwardly distributed through the lower cylindrical treatment zone 22 by means of distribution means, for example a flow distributor 23. The gas moving upward through the lower zone 22 flows directly into the central assembly zone 24, where it mixes with gases entering radially inwards through the upper treatment zone 12, and leaves the plant through the outlet 6. The central assembly zone 24 is under pressure, which is less than the pressure of the gases entering through inlets 14 and 21. Since the upper surface of the lower processing zone 22 is formed only by catalyst particles that move by gravity around the lower edge of the inner wall 17 of the transit, coagulant, there is no tendency for the upward gas flow into the transit zone 16. The flow will be absent, since the particles in the transit zone providing back pressure on the gas. In addition, a small amount of gas moving down in the transit zone will have greater pressure. than the pressure in the central assembly zone 24.
    The flow rate of column 13 through zones 12 and 22 is determined by the rate at which the particles leave zone 22 through exit 25. Particles leaving zone 22 can be directed to additional processing, such as drying, which is not the subject of this invention.
    A sampling device 26 may be used to sample particles in the transit zone 16. This device is also not the subject of the invention. It may contain a vessel 27 provided with a valve 28 and connected with a flange 29 to an outlet 30 having a distribution valve 31.
    FIG. 3 shows, on a larger scale, a cross section A-A in FIG. 2, which shows the shape of the annular machining zone 12, as well as the fact that the wedge-shaped wires 32 and 33 welded to the rods 34 and 35 to form sieves (4 and 10, respectively) have slots 36 whose size is smaller than the diameter of the catalyst particles, therefore, the gas passes through them, but there is no particle.
    权利要求:
    Claims (3)
    [1]
    Claim 1. An apparatus with a moving catalyst bed, comprising a housing consisting of two sections of different sections interconnected by means of a conical adapter, in the upper of which are perforated screens coaxially forming between them a catalyst zone in the form of an annular cushion of catalyst particles, moving under the force of gravity, and the gas distribution zone between the outer perforated screen and the casing wall with a radial supply pipe for the first treatment gas through the ring cushion into the inner zone of the inner
    a perforated screen and a second gas supply pipe located in the lower section, characterized in that, in order to intensify the process, the inner and outer perforated screens are equipped with transit elements made in the form of shells, the outer of which is fixed to the lower end on a conical adapter facing a large base to the upper section, and the internal transit element is installed with a gap Relative to the narrowing cylindrical wall of the lower section with the formation of an annular channel for the flow of particles of the roll congestion from one section to another, the height of which is equal to its width.
    [2]
    2. The apparatus according to claim 1, wherein the height of the internal transit element is at least three times the thickness of the ring cushion.
    [3]
    3. The device on PP. 1 and 2, in that the width of the channel for the flow of catalyst particles from one section to another is less than half the radial width of the ring cushion.
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    同族专利:
    公开号 | 公开日
    US4615792A|1986-10-07|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2303717A|1939-12-15|1942-12-01|Standard Oil Co|Regeneration of contact material|
    US3238122A|1964-01-17|1966-03-01|Socony Mobil Oil Co Inc|Hydrocarbon conversion process and apparatus useful therefor|
    US3647680A|1969-09-25|1972-03-07|Universal Oil Prod Co|Continuous reforming-regeneration process|
    US3725249A|1971-12-14|1973-04-03|Universal Oil Prod Co|Continuous reforming-regeneration process|
    US3839196A|1973-08-09|1974-10-01|Universal Oil Prod Co|Reactor-to-regenerator catalyst transport method|
    US3978150A|1975-03-03|1976-08-31|Universal Oil Products Company|Continuous paraffin dehydrogenation process|US4939314A|1988-12-19|1990-07-03|Mobil Oil Corporation|Method for on-stream low-pressure regeneration of an oligomerization catalyst from a fluid-bed reactor operating at high pressure with hydrocarbons in a non-liquid phase|
    US4945175A|1989-05-26|1990-07-31|Uop|Dehydrocyclodimerization process start-up procedure|
    US5091075A|1990-07-06|1992-02-25|Uop|Reforming process with improved vertical heat exchangers|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/727,152|US4615792A|1985-04-25|1985-04-25|Hydrogen circulation for moving bed catalyst transfer systems|
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