• 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:
    Particulate catalyst which has been used in a hydrocarbon conversion process such as catalytic reforming is regenerated in a moving bed regeneration zone (12). The catalyst being regenerated is passed into the top of the zone (12) and slowly moves downward as a dense bed (14, 19, 20) which is contacted successively with an oxygen-containing gas stream (31), a temperature-adjusting gas stream (30) and either a drying gas stream (37) or a chlorination gas stream (39) or both at different elevations within the regeneration zone (12). A key feature involves employing a portion of relatively hot combustion gas (26) withdrawn from one portion of the zone (12) as the temperature-adjusting gas stream (30) in a different portion of the zone after compression, with the remainder of the compressed combustion gas (27) being cooled (32) and recycled to the combustion zone as the gas stream (31). This eliminates the need to employ a heater to provide a suitable heating gas stream.
    公开号:SU1706375A3
    申请号:SU864027313
    申请日:1986-04-24
    公开日:1992-01-15
    发明作者:Раймонд Гринвуд Артур
    申请人:Юоп Инк (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for the regeneration of catalysts, in particular to methods for the regeneration of platinum-containing reforming catalysts.
    The aim of the invention is to increase the efficiency of the process by compressing a portion of the gaseous products of combustion produced to produce a process gas stream
    increased pressure, directing the produced gas stream to the heating zone located after the combustion zone, where it contacts the decarbonated catalyst coming from the combustion zone, cooling the rest of the process gas stream and directing it to the combustion zone as an oxygen-containing gas.

    cm
    The drawing schematically shows the reforming process in a moving catalyst bed.
    The reaction zone 1 usually contains three or four separate catalyst layers with intermediate heating in the case of carrying out the catalytic reforming or catalytic dehydrogenation reaction. The initial reagent stream enters the reaction zone via line 2. After contacting the catalyst particles under the reaction conditions under single or multiple conditions, the reactants and target compounds are removed from the reaction zone via line 3 and sent to the appropriate product utilization facilities. The catalyst solids are continuously or intermittently withdrawn from the reaction zone through pipe 1 and are directed down to the catalyst lift box 5. The catalyst is transported by gravity with the removal of the catalyst in the lower part of the reaction zone and the movement of the catalyst in the reaction zone from top to bottom. The catalyst withdrawn from the bottom of the reaction zone is replaced with fresh regenerated catalyst fed through line 6; Oxygenating gas, such as hydrogen or nitrogen, is fed into the catalyst lift collection through conduit 7 so as to transport the spent catalyst up through conduit 8. Then the spent catalyst enters the dedusting and separation vessel 9, where the catalyst particles and the transporting gas from the pipeline 7 separated in the form of a stream, which is removed, from the process via pipeline 10. The spent carbon-rich catalyst from separation vessel 9 is passed down through pipeline 11 to zone 12 p. regeneration.
    The catalyst within the regeneration zone is in the form of a dense compact mass, with each particle of the catalyst resting on the particles below. The catalyst particles gradually move down through the regeneration zone with a moving bed and pass through a series of zones in which they come into contact with various gas streams. In the upper part of the regeneration zone, the catalyst enters through distribution pipelines 13 into an annular catalyst layer enclosed between the inner porous lattice 15 and the outer cylindrical porous lattice 16. These lattices divide the upper portion of the regeneration zone into an annular volume with a catalyst located
    between the grids, and two reaction or gas transport volumes. The outer gas transmission volume is located between the outer grate 16 and the inner surface of the cylindrical vertical wall of the regeneration zone. The internal gas transmission volume is a cylindrical volume located inside the lattice 15-Top of the cylindrical inside
    0 gas transport volume
    closed with a perforated circular plate 17-B; preferably, the internal lattice 15 is growth-to-the-bottom in the lower part of the regeneration zone and
    5 reaches the lower cylindricality of the catalyst layer 18 held inside the HMweu part of the regeneration zone.
    At the top of the regeneration zone
    0 carbon is burned from the catalyst.
    Combustion is supported by a relatively low concentration of oxygen contained in the oxygen-containing gas stream supplied to the combustion zone through conduit 19. The gas flow supplied through conduit 19 enters the annular gas transport volume located outside the outer lattice 16 and spreads over the outer surface of the lattice 16 The gas flow from conduit 19 then passes through the catalyst bed and through the porous inner grid 15 into the cylindrical gas transport volume. This gas stream contains recycled inert impurities, such as nitrogen and water vapor, and combustion products, such as water vapor and carbon dioxide. Passing through the catalyst, the gas is heated by heat from the combustion of oxygen. The resulting gas stream at a relatively high temperature is removed from the cylindrical gas transport volume through conduit 20, through which gaseous combustion products are fed to conduit 21. Some of the combustion products are removed from
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    517 process by pipeline 22, and to save the required amount of combustion products. The rest of the gaseous products of combustion are directed to the pipe 23 and compressed by a fan or compressor. Thus, relatively hot combustion products are compressed to compensate for the pressure loss associated with gas recirculation through the regeneration zone.
    The first part of the compressed thus and still relatively hot combustion products is passed through the pipeline 25 in an amount regulated by a valve .6. This gas stream enters the regeneration zone through conduit 27 as a heating stream with a relatively high temperature, which in this case is also called a temperature control stream. This relatively high-temperature gas stream passes through a small lower suit of the ring layer of the catalyst, serving as a gallant zone, and then re-penetrates into the cylindrical gas transport volume located inside the wall 1 Carbon dioxide carbon ring oxy-ring ring / 3 installed in a ring-gas transmission system between the inner surface of the regeneration zone wall and the grid 16
    The remainder of the hot and compressed combustion product stream from line 23 is directed to conduit 19 and fed to a cooler 29, which is preferably an air-cooled apparatus. The gas stream from line 19 can also pass through heat exchanger Zi, in which indirect heat exchange is carried out with heating or cooling medium. Usually, heat exchanger 3 is not used when operating along the main axis, it is provided for the possibility of starting the regeneration zone in order to heat the catalyst to a temperature sufficient to maintain the conditions of spontaneous burning. Temperature-controlled gas is then supplied via conduit 19 to the regeneration zone in order to maintain the combustion of carbon located on the catalyst entering the

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    zoo rhe reiii gene. An incalable combustion of oxygen is mixed into the gas inside the cylindrical gas transport volume located inside the grid 15. Oxygen is introduced into the lower part of the regeneration zone, and it flows upward through the cylindrical catalyst bed and further into the lower part of the cylindrical gas transport volume. This method of adding oxygen is preferred. However, a certain amount of oxygen or all oxygen can be introduced by other methods, for example, by adding 1 9 to the line.
    In the lower section of the regeneration zone, the catalyst after treatment to remove carbon in the combustion zone and heat in the temperature control zone (heating) enters the chlorination zone, where it is limited to the form of a cylindrical catalyst layer 18, which occupies the entire volume of the cylindrical section of the catalyst regeneration zone. points. Chlorination of the catalyst is carried out using a stream of chlorinating gas fed to the regeneration zone through conduit 31 and distributed inside the catalyst bed through distribution devices 32, which may be perforated ducts or pipelines extending into the inside of the cylindrical catalyst bed. In a preferred embodiment, the chlorinating gas also contains oxygen, and this gas exits distributor 32 and flows to the upper parts of the regeneration zone. As the catalyst descends from the chlorination zone, it enters the drying zone, where it is held in the form of a cylindrical layer 33. The heated air from conduit 3 enters the lower part of the drying zone through conduit 35 and distribution pipe 36. The drying air is directed upwards in countercurrent to flow very slowly descending catalyst. Air oxygen from line 3 enters the cylindrical gas transport volume inside the cylindrical internal grid 15 for mixing with the combustion products. A portion of the air from conduit 3 flows through conduit 37 and is mixed with chlorine or another chlorine-containing substance to produce a stream of chlorinating gas.
    The low carbon content dried chlorinated catalyst leaves the regeneration zone through conduit 38 and enters bunker gate 39. This transfer can be made and adjusted using, for example, rotary sealing valves installed on line 38 or line 0 through which the catalyst from the bunker gate 39. The bunker gate 39 mainly operates as a sealing device to prevent air from the regeneration zone from mixing with hydrogen and hydrocarbon cages located in other AST X in the process of carbon conversion. Therefore, to blow off oxygen from the descending catalyst, pipeline M is supplied with nitrogen or another inert gas, which in a preferred embodiment, flows through pipeline 38 up into the regeneration zone. The regenerated catalyst is then transported via line 0 to the catalyst lift container 2. A stream of hydrogen gas from the line is preferably sent to tank k2 for a dual purpose, namely, to recover the metal components of the regenerated catalyst and liquefy the regenerated catalyst to transport it up the pipeline 6. and return to the reaction zone. The reducing gas is preferably hydrogen, although it can be used in light hydrocarbons, such as methane. The reduction can be carried out on a catalyst waiting to be transported in the lift tank, for example, as shown in the drawing or in a separate vessel. The reduction conditions depend on the type of catalyst used. When used as a reducing agent for hydrogen or methane at temperatures above 750 ° F (399 ° C), the use of elevated pressure is required. In some cases, reforming catalysts require temperatures above 950 ° F (5 ° C) for 60 minutes or more.
    The invention is illustrated by the following example.
    Example. The device with a radial gas flow, shown in the drawing, is used to regenerate used in catalytic
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    forming catalyst by beats, carbon precipitation through combustion. The catalyst used has a flow rate of kg / h and injects through line 11 at an ambient temperature of about 25 ° C. The catalyst used contains 0.38 May. 1 platinum and 0.9 May. chlorine on spherical particles of aluminum oxide with a diameter of 0.16 cm. The used catalyst contains 8% by weight of carbon. The regenerated catalyst after drying contains 0.05 May; carbon and 1.0 wt.% chlorine.
    In option I, the device is used in a low pressure and low temperature mode. The pressure is 0.5 kPa. The temperature of the bulk r in pipelines 21 and 25 is equal, and in the pipe 19 - 7b C. The temperature of this gas stream is controlled by means of cooling means 30.
    In embodiment II, the device is used under preferred or optimal conditions; pressure is 2kl, 2 kPa; gas temperature in pipelines 21 and 25 is 520 ° С, and in pipe 19 - 7b C.
    In option III, the device operates under conditions of high pressures and temperatures: —pressure differently 1551 kPa; gas temperature in pipelines 21 and 25 is equal to 526 C, and in the pipeline 19 We.
    On average, the residence time of the catalyst in the combustion zone should be 55 minutes. After the catalyst leaves the combustion zone, it has a temperature equal to the temperature of the gas in stream 19). The catalyst is then heated to a predetermined chlorination temperature, which is equal to the temperature of the gas in stream 25. In all examples of the example, the chlorination gas has a flow rate of kg / h. Chlorination gas contains 3% by volume of water, 0.15% of progressed chloride and the rest is air. Before passing into the chlorination zone, it is heated by an electric heater. The average total residence time in the chlorination zone is 2.75 m. Chlorination serves to redistribute platinum, which is agglomerated during the carbon burning stage due to high localized temperatures. The final step before removing the catalyst is drying using air from line 35 at a flow rate of 80.25 kg / h and temperature.
    Table 1 shows the mass and volume flow rates of the gas passing through pipelines 21, 25 and 19 in each case. The flow rate of the total gas flow coming out of the pipeline can be easily calculated from the difference. The total flow rate of air loaded into the process is equal to the total flow rate of gas exiting through the pipeline 19. The composition of the gas in the pipelines for each option is listed in Table 2.
    Despite the large differences in flow rates, they are essentially the same.
    In all three variants, a temperature profile will be created inside the bed of the catalyst in the combustion zone, which will be within 7b-b75 ° C. The indicated gas temperatures represent the gas volume temperatures in the total gas flow, which is used as a cooling medium. It remains relatively constant in temperature, despite changes in other operating parameters, such as pressure.
    Thus, when using the method according to the invention, there is no need to use a heater to obtain an appropriate heating gas flow, which makes it more economical.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    Method for regeneration of a platinum-containing reforming catalyst, including passing a coked catalyst from top to bottom in the regeneration zone as a dense layer, contacting the catalyst with an oxygen-containing gas in the combustion zone located inside the regeneration zone, until carbon is completely burned, removing gaseous products of combustion from the regeneration zone, passing decarburized catalyst through the chlorination zone located in the regeneration zone, and contacting the catalyst in this zone with chlorinating gas stream containing chlorine-containing substance, the removal of the catalyst from the Regene zone
    radios, which, in order to increase the efficiency of the process, part of the gaseous products of combustion are compressed to produce a process gas stream under increased pressure, 5-25% of the resulting gas stream is directed to the heating zone located after the combustion zone. With a decarbonized catalyst coming from the combustion zone, the rest of the process gas stream is cooled and sent to the combustion zone as an oxygen-containing gas.
    Table 1 Gas consumption
    Teblitse2
    40
    Gas composition
    II
    Carbon dioxide13, 3
    Nitrogen71, b
    Water1,3
    Oxygen. ten
    Carbon dioxide13, 3
    Nitrogen, 71,
    1706375 | Continued tAPl. 2
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    同族专利:
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    引用文献:
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    US3238122A|1964-01-17|1966-03-01|Socony Mobil Oil Co Inc|Hydrocarbon conversion process and apparatus useful therefor|
    US3652231A|1969-09-25|1972-03-28|Universal Oil Prod Co|Reconditioning system for moving column of reforming catalyst|
    US3725249A|1971-12-14|1973-04-03|Universal Oil Prod Co|Continuous reforming-regeneration process|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/727,151|US4578370A|1985-04-25|1985-04-25|Gas circulation method for moving bed catalyst regeneration zones|
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