• 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:
    1491558 Fluidized bed furnace FIVES-CAIL BABCOCK 3 Feb 1975 [14 Feb 1974] 4548/75 Heading F4B [Also in Divisions B 1 and C5] Granular solid materials are reacted at such a temperature that agglomerates are formed in a deep fluidized bed connected to a secondary bed through a submerged passage, a bed support extending below both beds and being upwardly inclined at least at part of its length beneath the secondary bed, and means are provided to move agglomerates over the support to emerge from the surface of the secondary bed. The secondary bed may be formed in gas-tight enclosure 11 so that beds are maintained in hydrostatic equilibrium. The support may be the upper run of an inclined chain grate 15, and the end of the grate may emerge from the secondary bed or the secondary bed may be level with the end of the grate. Agglomerates S carried out of bed fall into a water sealed shoot 22. Fines carried over in gases exiting from the outlet 10 are returned from a cyclone separator 28. The apparatus may be used for gasification of coal or other material, or in the manufacture of cement.
    公开号:SU1085500A3
    申请号:SU752112953
    申请日:1975-02-13
    公开日:1984-04-07
    发明作者:Годель Альбер
    申请人:Фив-Кай Бабкок (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the design of a fluid bed apparatus and can be used to gasify a fuel, produce clinker in a cement industry, and to carry out reactions that occur at temperatures that cause the reaction products to self-adhere. A known method of carrying out processes in a fluidized bed of solid reagent proceeding during heating with the formation of agglomerates includes fluidizing the solid reagent in the main fluidization chamber and the subsequent transportation of agglomerates using a conveyor to the discharge chamber G1.3. The disadvantage of this method is that when it is carried out large reagent loss. A known apparatus for carrying out processes in a fluidized bed includes a main fluidized bed chamber, an agglomerate unloading chamber with means for maintaining and controlling the hydrostatic pressure therein, adjacent to the main chamber and separated from a non-vertical dividing partition, a gas distribution grid made in the form of an inclined-mounted conveyor, the upper end of which is located in the discharge chamber and the pressure sections for the fluidizing gas located below the conveyor t l. The disadvantage of this device is that it is impossible to carry out a method of carrying out processes in the fluidized bed that occur during heating to form agglomerates, especially when the fluidized bed is deep. The purpose of the invention is to facilitate the discharge of the agglomerates and reduce the loss of reagent in the discharge chamber. The goal is achieved by the fact that, according to the method of carrying out processes in a fluidized bed of solid reagent, occurring during the heating with the formation of agglomerates, including the fluidization of the solid reagent in the main chamber of the scraper, and the subsequent transportation of the agglomerates by means of a conveyor to the discharge chamber, on a conveyor belt Fluid fluid nor solid reagent under pressure. In an apparatus for carrying out processes in a fluidized bed, including a main fluidized bed chamber, an agglomerate unloading chamber with means for maintaining and regulating the hydrostatic pressure in it, adjacent to the main chamber and separated from it by a vertical dividing partition of the gas distribution grid, made in the form of, inclined a conveyor, the upper end of which is located in the discharge chamber, and the pressure sections for fluidizing gas, located below the conveyor, are lower The i-edge of the vertical partition is located below or at the same level as the upper end of the conveyor. Depending on the specific use case, the proposed apparatus may contain: means, for example nozzles, for blowing into the base layer, above the substrate level, reaction gases, which in some cases it is advisable to heat to a temperature exceeding the temperature of the gases blown through the substrate, means for supplying pneumatically into the main layer of granular substances by dispersing over the surface or blowing into the layer, means for dedusting gases coming out of the reaction zone by passing them through cyclones or other devices, and for reintroducing, if necessary, the solid fractions obtained as a result of separation into the main fluidized bed, means for preheating fresh granulated substances due to heat exchange with gases coming from the reaction zone, means for treating the original carbon-containing substances are strongly heated by air or oxygen with the addition of water vapor. Figure 1 shows the proposed installation, the longitudinal vertical pa3pei3, figure 2 - section aa in Fig. 1, figure fig. 3 - section bb in figure 1. The apparatus comprises a main fluidized bed chamber 1 formed by the front wall. 2 and the rear
    a wall 3, two side walls 4, a bottom 5 and a lid 6. In the lower part of the rear vertical wall 3 there is a rectangular opening 7, which is made to the bottom 5 and adjacent to which is an agglomerate unloading chamber 8 formed by two walls 9 located on both sides holes 7, and a lid 10, located at the level of the upper edge of this hole. The upper part of the hole 7 is blocked by a vertical dividing partition 11, forming the lower continuation of the wall 3.
    Chamber 1 Contains a floor 12, installed with a lift towards the rear, in which a longitudinal slot 13 is made, having a width equal to or approximately equal to the width of the hole 7. The slot 13 is closed by a grille 14, formed by the молth straight upper line of the endless chain 15 and a free-hanging lower branch 16, Infinite chain 15 passes through the front roller 17 placed in a hole made in the front wall 2 and through the rear drum 18 which rests on the transverse wall 19. The upper branch of the endless chain 15 forms a subdivision A discharge grid 14 with upward movement from the front to the rear part, and pressure distribution sections 20 are installed to inject the fluidizing gas below the bottom surface of this moving grid.
     8 is closed at its rear end by a transverse wall 21 and between the walls 21 and 19 there is a transverse partition 22, which, like the wall 21, is immersed at its lower end in a water tank 23 forming a slag collector with a hydraulic plug for the channel defined by the walls 9, 21 and a partition 22.
    Through each of the two side walls 4 defining the main chamber 1, there is one row of nozzles or nozzles 24 serving to feed gas into the chamber 1 for heating and / or heat treatment, and the other, located above, a row of nozzles 25 intended for pneumatic feeding ground matter. A nozzle 26 passes through the upper part of the front wall 2, which also serves to feed the granulated material into the chamber 1.
    A gas removal pipe 27 passing through gasket 6 of chamber 1 leads to a cyclone 28 having an upper pipe 29 to remove gas and a lower pipe 30 to return solids to chamber 1. The pipe 27 has a branch 31 located above its entry point cyclone 28.
    Consider the mode of operation of the installation in the case of its use for the gasification of fuel, coal or carbon-containing substances.
    In this application, the gasifiable substance supplied to the installation forms two layers in the latter: a deep layer in chamber 1 and a shallow layer in chamber 8, while the surface of the latter is approximately at the level of the lower edge of partition 11, which is preferably cooled by circulating water. Both these layers lie on the lattice 14 formed by the upper branch of the infinite chain 15.
    The distribution sections 20 blow hot air, having, for example, a temperature of 100-150 ° C, under the grate 14. This hot air passes through both boiling beds, and since pipe 27 is the only outlet in the 1st channel all The apparatus, in connection with the presence of a hydraulic plug, the gas released in chamber 1 can only go out through a deep fluidized bed and, thus, contributes to the gasification of the fuel forming this layer, as well as directly supplied air to this layer. As a consequence, there is an overpressure in the free surface of the shallow layer, and both layers are thus in equilibrium.
    Since gas production with a high calorific value gas requires a significant amount of heat to be supplied to the deep layer through nozzles 24, air is blown at a temperature of about 500 ° C, much higher than the air temperature supplied by the distribution sections 20, which prevents the impact on lattice too high temperatures.
    In operation, fuel is supplied to the installation either by directly blowing nozzles 25 into the bed, or by spraying over the surface through nozzles 26, or by these two methods. The gaseous products, which are collected in the upper part of chamber 1, exit from it through pipe 27 and enter the dedusting cyclone 28. The solid phase returns to the deep layer through pipe 30. 30 and the gas phase goes through pipe 29 to the place of storage or use, or also to one or more other separators, cyclones or similar devices connected in series with the cyclone 28. Branch 31 serves to supply fuel through pipe 27, in which the gaseous products are heated by heat recovery through direct heat exchange between them and with Mode fuel. The self-sealing ashes, which are formed during the operation of the installation, are deposited on the movable grid 14, are lifted together with it and are transferred from the deep to the non-shallow layer, exit through the upper surface of the latter and fall between the partitions into the tank 23, which forms a hydraulic plug or water barrier. In the example shown, the top point of the grille 14 is approximately at the level of the lower edge of the partition 11, which corresponds to the level of the second layer. In other applications, it is possible to create a difference between these levels. For example, the top point of the grid 14 may be above the bottom edge of the partition 11 so that the slags are completely exposed to the surface of the second shallow layer. In a similar manner, the lower edge of the partition 11 can be located at a lower level than the level of the second layer. In any case, the channel through which the two layers communicate at their base is a recessed channel. 06 It is advisable to blow the surface of slags that come to the surface together with the grate through pipe 32 to improve their dust control. The side fuel injection nozzles 25 may be arranged differently with respect to the air injection pipes and, for example, be at the same level with them. In addition, fresh fuel may not be supplied pneumatically, but, for example, mechanically. One or more dust removal cyclones or other separators can be used to carry out heat exchange between gaseous products and fresh fuel for heat recovery, as is commonly done in the cement industry. In order to recover heat, it is also possible to carry out heat exchange between gaseous products and injected air or another gas. In another embodiment, over the deep layer of solids in the course of the reaction, a second boiling layer is formed to treat the gases coming out of this layer, and the treatment may consist, for example, in desulfurization, in particular, in the case of gasification of fuel . The movable grill 14 can be tilted only on parts of its stroke — on the rear. It can be of a type other than a hanging chain lattice, and the proposed device for removing agglomerates formed during melting can be constructed using, for example, a shaking grate or a composite lattice containing one part in the form of a lattice with a horizontal chain and part with an inclined auger, which is a continuation of the horizontal grid. During gasification, it is possible to completely or partially replace air with a mixture of oxygen and water vapor.
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    权利要求:
    Claims (2)
    [1]
    1. The method of carrying out processes in the fluidized bed of a solid reagent, proceeding during heating with the formation of agglomerates, including fluidization of a solid reagent in the main fluidization chamber and subsequent transportation of the agglomerates using a conveyor to the discharge chamber, about t and -. characterized in that, in order to facilitate the unloading of agglomerates and reduce reagent losses in the loading chamber, the mode of fluidization of the solid reagent under pressure is supported on the conveyor.
    [2]
    2. An apparatus for carrying out processes in a fluidized bed, including a main chamber with a fluidized bed, an agglomerate discharge chamber with means for maintaining and regulating hydrostatic pressure in it, adjacent to the main chamber and separated from it by a vertical dividing wall, a gas distribution grill made in the form of an oblique installed conveyor, the upper end of which is placed in the discharge chamber, and pressure distribution sections for fluidizing gas located below nsportera, characterized in that, in order to facilitate discharge of the agglomerates and to reduce loss of reactants in the discharge chamber, the lower edge of vertical baffle located below or at the same level as the upper end of the conveyor.
    类似技术:
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    US4208307A|1980-06-17|Purification of coke
    同族专利:
    公开号 | 公开日
    US3982884A|1976-09-28|
    CS207338B2|1981-07-31|
    CA1032735A|1978-06-13|
    PL94961B1|1977-09-30|
    DE2506080A1|1975-08-21|
    DD117613A5|1976-01-20|
    FR2261051B1|1980-08-08|
    IN141130B|1977-01-22|
    DE2506080C2|1987-01-29|
    FR2261051A1|1975-09-12|
    GB1491558A|1977-11-09|
    ZA75741B|1976-01-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1832092A|1926-11-20|1931-11-17|Delaware Lackawanna & Western|Gas producer|
    US2716598A|1951-02-06|1955-08-30|Du Pont|Preparation of carbon monoxide and hydrogen by partial oxidation of carbonaceous solids|
    US2776879A|1952-01-02|1957-01-08|Hydrocarbon Research Inc|Gasification of solid carbonaceous fuel|
    US2866696A|1953-10-29|1958-12-30|Cie Ind De Procedes Et D Appli|Process for the gasification of granulated fluidized bed of carbonaceous material, over moving, sloping, horizontal, continuous grate|
    FR1092540A|1953-10-29|1955-04-22|Cie Ind De Procedes Et D Appli|Improvements in processes for carrying out chemical reactions in the fluidized phase and device for their implementation|DK172675A|1975-04-22|1976-10-23|Niro Atomizer As|PROCEDURE FOR PNEUMATIC TRANSPORT OF PARTICLE OR POWDERED MATERIAL AND PLANT FOR USE IN THE PERFORMANCE OF PROCEDURE|
    DE2624302C2|1976-05-31|1987-04-23|Metallgesellschaft Ag, 6000 Frankfurt, De|
    US4174949A|1977-08-29|1979-11-20|Cmi Corporation|Burner and exhaust control assemblies for use with an apparatus for conveying particulate material|
    GB2034679B|1978-11-14|1982-05-19|Coal Industry Patents Ltd|Heating slurries|
    FR2528543B1|1982-06-15|1985-03-15|Fives Cail Babcock|
    FR2551453B1|1983-08-31|1985-10-11|Fives Cail Babcock|COAL GASIFIER IN HIGH-PRESSURE FLUIDIZED BED|
    GB2150040B|1983-12-07|1988-04-27|Onoda Cement Co Ltd|Thermal decomposition furnace for waste tyres|
    DE19536920C2|1995-10-04|1998-10-29|Meurer Franz Josef|Method and device for dedusting the reaction gas of a gasification reactor|
    US6042369A|1998-03-26|2000-03-28|Technomics, Inc.|Fluidized-bed heat-treatment process and apparatus for use in a manufacturing line|
    CN106032897B|2015-03-16|2018-12-25|曹登林|A kind of less boiler|
    RU2697472C1|2019-03-13|2019-08-14|Сергей Айдынович Адыгезалов|Method of thermo-oxidative coking and device for its implementation|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR7404956A|FR2261051B1|1974-02-14|1974-02-14|
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