• 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:
    This invention relates to a method for the production of anhydrous alumina having a desired alpha -conversion from alumina trihydrate. This method is directed to production of anhydrous alumina having a desired alpha -conversion from alumina trihydrate in which water is removed in a precalcining zone wherein the alumina trihydrate is heated to a temperature below 450 DEG C. Then, the precalcined dehydrated alumina is recrystallized to alpha -alumina in a reaction chamber by directing an oxygen containing gas to the reaction chamber, mixing and suspending the precalcined alumina and fuel in the oxygen containing gas and feeding the mixture to a combustion zone, followed by exothermal recrystallization of the alumina which is initiated by rapidly heating the precalcined alumina by burning the fuel in the oxygen containing gas in the hot combustion zone and withdrawing the recrystallized alumina from the top of the reaction chamber suspended in a combustion gas stream. The recrystallized alumina is then separated from the gas stream and cooled to produce anhydrous alumina having the desired content of alpha -conversion.
    公开号:SU932979A3
    申请号:SU792755653
    申请日:1979-04-19
    公开日:1982-05-30
    发明作者:Эрик Раахауге Бенни
    申请人:Ф.Л.Смидт Энд Ко А/С (Фирма)；
    IPC主号:
    专利说明:

    parts of the calcification chamber below the grate. The closest to the technical clh proposed and the effect achieved is a method of producing alumina by dehydrating the raw material, heat treating the calcination chamber with the fuel supply to the lower part of the chamber and oxygen-containing gas from the bottom centrally to the chamber and cooling the target product, the fuel and the dehydrated product being fed from This side of the chamber is in the form of a cross flow 2. The duration of the heat treatment process according to this method is 2-3 minutes, which is also unsatisfactory. The apparatus for carrying out the conventional method comprises a cyclone preheater connected to a calcination chamber, provided with pipes for supplying dehydrated products and fuel located at an angle to each other in one side wall of the chamber, and a pipe for supplying oxygen-containing gas, located in the center of the bottom of the chamber, and a cooler connected to the calcination chamber. The purpose of the invention is to reduce the duration of the process. The goal is achieved by the fact that in the method of producing alumina by dehydrating the raw material, heat treating the dehydrated product in the calcination chamber — with supplying fuel to the lower part of the chamber and oxygen-containing gas from the bottom center — and cooling the target product, and feeding the fuel and dehydrated product from the same side of the chamber as a cross-flow, the dehydrated product is fed to the lower part of the caner. After the separation of alumina, the gases leaving the heat treatment zone can be used to dehydrate the raw material. Alumina trihydrate can be used as a raw material. Dust separated from gases leaving the dewatering zone can be fed into the stream of gases from the waste treatment zone in which the target product is suspended. The decontamination step is preferably carried out in a multi-stage cyclone preheater. The air used by 9 4 at the stage of cooling the target product can be applied to heat treatment as an oxygen-containing gas. If the dewatering is carried out in a multi-stage cyclone preheater, then the material obtained in the latter along the off-gas cyclone can be divided into two streams, one of which is fed to the ascending pipe of the last one along the off-gas cyclone, and the other stream along with the material , separated from the air, is subjected to further cooling, and the air is fed to the heat treatment as oxygen and gas. Before suspending in the cooling air, the second stream of material and material. separating from heat treatment exiting can be fed to the mixer. The invention makes it possible to shorten the heat treatment time to 0.5-5 seconds. The proposed method is carried out in a device containing a cyclone preheater connected to a calcination chamber, equipped with pipelines for supplying dehydrated product and fuel angled to one another in one side wall of the chamber, and an pipeline for supplying oxygen-containing gas located in the center of the bottom of the chamber , and a cooler connected to the calcination chamber, the distinguishing feature of which is that the pipeline DGG for supplying the dehydrated product is located in the low part to Calcination chambers above the fuel line. It is advisable to make the walls of the lower part of the calcination chamber inclined inwards. Discharge Pipeline: A waste gas dehydration stage may be associated with a device for supplying a mold to the ascending pipe of the calcination chamber. FIG. shows a device for implementing the proposed method, one option; in fig. 2 - the same, another option. The device of FIG. 1 contains a calcination chamber 1. equipped with a pipeline 2 for supplying oxygen-containing gas located in the center of the bottom of the chamber. In addition, chamber 1 is provided with piping 3 for a basement.
    fuel line and a pipe 4 located above it for supplying dehydrated product from cyclone 5, the upper part of which is connected through pipelines 6 and 7 with cyclone 8 for drying raw materials supplied by pipeline 9, and with cyclone 10 for separating the target product from gases. The upper part of the cyclone 8 is provided with a pipe 11 for removal of flue gases, and the lower part of the cyclone 10 is connected to the cooler 12 via a pipe 13. The cooler 12 is equipped with a pipe 14 for withdrawing the target product. The calcination chamber 1 is connected via a pipe 15 to a cyclone 10, and the pipe 15 can be supplied with a pipe of 16 dp of feed supply.
    The lower part of the cyclone 8 is connected to the upper part of the cyclone 10 through line 7.
    Another embodiment of the device of FIG. 2 has the following differences from the previous one. On the pipeline 17 valves are installed. The electrostatic precipitator 18 separates the dust. The lower part of the cyclone 8 is provided with an additional pipe 19, directly connected to the cooler 12, valves 20 and 21 are installed in the pipes 17 and 19. The pipe 14 for withdrawing the desired product enters the pipe 22, through which cold air is supplied. Pipeline 22 is connected
    with an additional cyclone 23 located under the calcination chamber 1. The Nihsh part of the cyclone 23 is provided with a pipe 24 for removing solids separated from the air stream c. cyclone 23.
    Example. The above alumina is carried out in a device containing a cylindrical calcification chamber with a height of 3800 mm and an inner diameter of 600 mm. Light fuel oil is used as fuel and air is supplied in an amount that provides a speed of 3.8 m / s in the calcination chamber.
    Moist alumina trihydrate containing 12% free water.
    dehydrate with the exhaust gases of the calcination chamber in the cyclone preheater shown in FIG. 1. In this case, the free water is removed and dry alumina trihydrate is obtained, the calcination loss of which is 34.9%. After further heating in the preheater, raw materials with a temperature of 400-450 ° C are fed into the chamber
    calcification. In this case, the loss from calcination is about 3-6%. The dehydrated product is fed to the lower part of the chamber, in which it is brought into contact with the fuel supplied slightly below the feed point of the dehydrated product (Fig. 1). The mixture of dehydrated product with fuel is suspended in the combustion air supplied in the middle of the bottom of the chamber. The temperature in the chamber is measured in three places. The average temperature in the reactor is given in table. one.
    By changing the amounts of fuel and air supplied, it is possible to regulate the average temperature in the calcination chamber and thus the content of f / -Oxy aluminum in the target product.
    The target product is carried by gases from the chamber. calcifications; It is then separated from the gases and cooled.
    After cooling, the content of the alumina in the target product and the loss from calcination are determined. . The results are summarized in table. I.
    In tab. Table 2 lists the content of the alumina ob-oxide in various fractions, and in Table. 3 - distribution of minerals products by X-ray diffraction patterns.
    In Examples 1-5, the loss from calcination is 0.1-0.5%, and the yield of the desired product is about 200 kg / h.
    In winners 6-8, the loss from calcination is 0.4-0.5%, and the time for heat treatment is 0.8-1.0 s.
    The specific consumption of theopic in the above examples is 750,800 kcal / kg alumina.
    eight
    Table 1
    4 5
    1335
    17 9 1260
    1510 75.2 75.7 76.2 79.0 77.6
    6 7 8 1435 40.5 43.7 45.6 50.5 47.4 16.7 14.5 14.5 13.6 14.5
    os-
      5-, 8g9- AlgO Y, & - in-AljOg
    权利要求:
    Claims (3)
    [1]
    Invention Formula
    J. A method of producing alumina by dehydrating, heat-treating the dehydrated product in the calcination chamber with the supply of nausea in the lower part of the chamber and oxygen-containing gas S1SHZU centrally in the chamber and cooling the target product, the fuel and the dehydrated product are fed from the same chamber in the form of a cross flow , characterized in that, in order to reduce the duration of the process, the dehydrated
    Powder0.89
    Powder0.88
    Intermediate - 0.80 ny
    Sandy
    1.02 Sandy 0.96,
    Table 2
    T a b l and c a 3
    j, S-, e -
    the product is fed to the bottom of the chamber,
    [2]
    2, an alumina production apparatus comprising a cyclone preheater connected to a chamber
    Calcination, equipped with pipelines for supplying the dehydrated product and fuel located at an angle to each other in one side wall of the chamber, and a pipeline for supplying oxygen-containing gas located in the center of the chamber bottom, and a cooler connected to the calcination chamber, characterized in that In order to reduce the process duration, the pipeline for supplying the dehydrated product is located in the lower part of the calcination chamber above the pipeline for supplying fuel.
    [3]
    3. The device according to claim 2, from l and the fact that the walls of the lower part of the calcination chamber are inclined inward.
    Sources of information taken into account in the examination
    1. Patent of the USSR No. 668578, cl. B 01 J 8/24, 1968.
    2. Review information. New technology and equipment of alumina production abroad. M.,
    1977, p. 19, fig. four.
    nineteen
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    同族专利:
    公开号 | 公开日
    JPS54151597A|1979-11-28|
    FR2423445A1|1979-11-16|
    NL7903123A|1979-10-23|
    US4529579A|1985-07-16|
    DE2916142A1|1979-10-31|
    IN150912B|1983-01-15|
    NO791174L|1979-10-23|
    ES479716A1|1980-06-16|
    BR7902452A|1979-10-30|
    DE2916142C2|1983-01-27|
    YU44842B|1991-04-30|
    YU223982A|1986-08-31|
    ES482578A1|1980-04-16|
    GB2097903B|1983-03-23|
    GB2097903A|1982-11-10|
    AU4631079A|1979-10-25|
    AU533515B2|1983-12-01|
    MX151661A|1985-01-30|
    FR2423445B1|1983-08-05|
    HU180947B|1983-05-30|
    引用文献:
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    EA010273B1|2002-12-23|2008-08-29|Оутокумпу Текнолоджи Ой|Process and plant for producing metal oxide from metal compounds|GB745552A|1952-06-12|1956-02-29|Dorr Oliver Inc|Process of calcining finely divided solids|
    FR1080901A|1952-06-12|1954-12-14|Dorr Co|Method and apparatus for calcining alumina|
    US3057680A|1958-03-11|1962-10-09|Metallgesellschaft Ag|Method of carrying out heat-consuming reactions|
    DE1092889B|1958-03-11|1960-11-17|Metallgesellschaft Ag|Process and device for carrying out heat-consuming reactions between solids and gases according to the fluidized bed principle|
    FR1248038A|1959-10-28|1960-12-09|Electrochimie Electrometallurg|Anhydrous aluminas manufacturing process|
    FR1292741A|1960-06-24|1962-05-04|Metallgesellschaft Ag|Process for the calcination of alumina hydrate|
    DE1146041B|1960-06-24|1963-03-28|Metallgesellschaft Ag|Calcining alumina hydrate|
    FR1295554A|1961-04-28|1962-06-08|Electrochimie Soc|Device for the production of anhydrous aluminas|
    US3452968A|1966-10-12|1969-07-01|Ishikawajima Harima Heavy Ind|Roasting process of fine ore and a device therefor|
    GB1143880A|1967-06-16|1900-01-01|
    GB1428680A|1972-12-11|1976-03-17|Smidth & Co As F L|Calcination of pulverous material|
    JPS5716927B2|1974-03-11|1982-04-08|
    GB1463124A|1974-06-18|1977-02-02|Smidth & Co As F L|Calcination of pulverous material|
    DE2629082C2|1976-06-29|1985-09-05|Krupp Polysius Ag, 4720 Beckum|Method and device for the heat treatment of fine material|
    DE3008234A1|1980-01-23|1981-07-30|Aluterv-EKI Forschungs-, Entwurfs-u.Generalauftragnehmer-Zentrale der ungar. Aluminiumwerke, Budapest|METHOD AND SYSTEM FOR BURNING FINE-GRAINED GOODS|DK157442C|1982-12-07|1990-06-05|Smidth & Co As F L|PROCEDURE AND APPARATUS FOR CALCINATING PHOSPHATE|
    FR2549816B1|1983-07-28|1985-11-15|Fives Cail Babcock|CALCINATION PLANT FOR THE PRODUCTION OF SEVERAL QUALITIES OF ALUMINA AND METHOD FOR OPERATING THE SAME|
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    AU645509B2|1989-11-27|1994-01-20|Alcan International Limited|Calcination process for the production of alumina from alumina trihydrate and apparatus therefor|
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    法律状态:
    优先权:
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    GB1568978|1978-04-20|
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