• 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 clear-alkali metal silicate solution is obtained by passing an aqueous alkali metal hydroxide solution through a vertical tube reactor containing crystalline silica without mechanical stirring means.
    公开号:SU1311615A3
    申请号:SU833576496
    申请日:1983-04-14
    公开日:1987-05-15
    发明作者:Метцжер Жан；Лекул Анри；Коломб Филипп；Войцик Жан
    申请人:Продюн Шимик Южин Кюльман (Фирма)；
    IPC主号:
    专利说明:

    1, 13
    The invention relates to methods for preparing solutions of silicate alkali metal by reacting silica with an alkaline solution.
    The aim of the invention is to simplify the method
    Dimension 1, Into a heat-insulated vertical nickel pipe with an inner diameter of 90 mm and a length of 6 m, 53 kg of quartz sand with an average particle size of 300 microns is introduced. Then for 1 h 20 min, water solution of sodium hydroxide is passed with a content of 19.6 wt.% Na,., 0 and at a flow rate of 50 l / h, and the transmission rate is 7.9 m / h. The temperature in the pipe is maintained at 225 ° WITH,
    A solution of sodium silicate containing g / L: 194 and 485 SiOj is injected into the bottom of the reactor, the ratio being 2.5.
    Unreacted sand remains in the reactor where fresh sand has been loaded for the subsequent reaction,
    Example 2 Into a thermally insulated nickel vertical pipe with an inner diameter of 90 mm and a length of 2 m, quartz sand is fed with an average particle size of 300 μm at a flow rate of 22 kg / h, as well as a heated aqueous sodium hydroxide solution containing 11.2 wt.% Of calculation of 69 l / h of solution or 9 kg / h of Na, jO. Alkaline solution is passed at a speed of 10.8 m / h through a layer of sand located in the pipe. The pipe support at 220 C,
    The silicate diluent from the bottom of the reactor contains, g / l: 125Na20 and 306 SiOg, and the ratio of SiO2 / is 2.45.
    Example 3. Silica was continuously supplied to the pipe in the same way as in Example 2 with a flow rate of 27 kg / h and an aqueous solution of sodium hydroxide containing 17.6 wt.% NagO at the rate of 50 g / l solution corresponding to 11 kg / h. The alkaline solution was passed at a rate of 7.9 m / h through a sand layer located in a pipe, silica is a quartz sand with a particle size of 850 µm. The temperature of the reactor is maintained at 218 ° C. The silicate solution formed from the bottom of the reactor contains, g / l: 175
    five
    0
    five
    61
    0
    five
    0
    45
    50
    55
    5 .. .2
     and 429 SiO-2, and the ratio
    Si02. is 2.45,
    Example 4 Similarly to example 2, silica is continuously fed at a rate of 8.4 kg / h and an aqueous solution of sodium hydroxide containing 19.6 wt.% Naj, 0 at a rate of 33 l / h of solution or 8.28 kg / h, Alkaline. the solution is passed at a speed of 5.2 m / h through a layer of sand formed in the pipe. Silica is a silica sand with a grain size of 300 microns. The temperature in the reactor is maintained at 1, the silicate solution entering from below contains, g / l: 197 NagO and 200 SiO, and the ratio is 1.01 5,
    Example 5 Analogously to example 2, silica is continuously fed into the pipe at a flow rate of 25 kg / h and an aqueous solution of sodium hydroxide containing 23.4 wt.% At the rate of 40 l / h of solution or 17.1 kg / h. The alkaline solution is passed at a rate 6.3 m / h through a layer of sand formed in the pipe, silica is silica sand with an average particle size of 300 µm. The temperature in the reactor is maintained at 190 ° C. The silicate solution entering from the bottom contains 226 g / l and 454 g / l SiO, the ratio SiOg / Na O is 2.0,
    Example 6.B a vertical pipe made of thin steel, equipped with a double jacket with an internal diameter of 90 mm and a length of 2 m, is indispensable. silica is fed at a rate of 23 kg / h and a solution containing J4.9 wt,% and 20 g / l at the rate of 50 l / h of solution or 9.6 kg / h of Na,., 0, respectively. The alkaline solution is passed at a speed of 7, 9 m / h through a layer of sand formed in the pipe. Silica was quartz sand with an average particle size of 300 μm. The temperature in the pipe is maintained at 218 ° C. A certain pressure is maintained in the reactor by means of an adjustment. The solution formed from the bottom of the reactor contains g / l: and 384 SiOj, the ratio of SiO2 / Na20 is 2.4.
    Example 7 Into a tube similar to Example 2, silica is continuously supplied at a rate of 21 kg / h and an aqueous solution of sodium hydroxide, containing 16.7 weight,% at the rate of 50 l / h.
    313
    solution or 10.5 kg / Na20, respectively. The alkaline solution is passed at a speed of 7.9 m / h through a layer of sand formed in the pipe. Silica is a quartz sand with an average grain size of 130 microns. AT
    the reactor is kept at 190 s. The resulting silicate solution contains 165 g / l and 338 g / l of SiO and the ratio is 2.,.,
    Example 8. Silica with a flow rate of 31 kg / h and an aqueous solution of potassium hydroxide, containing 26.7 wt.% At the rate of 50.l / h of solution or 17.7 kg / h K, jO were continuously fed into the tube of Example 2. The alkaline solution is passed at a rate of 7.9 m / h through a layer of sand formed in the pipe. Silica is silica sand with an average particle size of 300 µm. The temperature in the reactor is 195 ° C. The resulting silicate solution contains, g / l: 264 and 462 SiO, and the ratio is 1, 75.
    Example 9. In the upper part of the reactor, made in the form of a vertical cylindrical tube of ordinary steel, carefully insulated from the environment with an internal diameter of 90 mm and a height of 6 m, give 13.3 kg / h of quartz sand with an average particle size composition of 300 microns at a temperature equal to the ambient temperature.
    „Tala and its rapture comprehends h
    In the upper part of the same reactor.
     01 g / using sand coarsely above the sand layer 33.6 kg / h
    mole instead of finely divided silicon oxide (save energy for crushing and therefore, investment), eliminating mixing
    a concentrated aqueous solution of sodium hydroxide containing 19.8 wt.% or 6.65 kg / h of Naj, 0 at a temperature of 192 C. The internal solution is passed at a speed of 4.1 m / h through a layer of sand;
    This alkaline
    homogeneous and exothermic mixing of 17.9 kg of concentrated aqueous sodium hydroxide solution containing 37.2% by weight and brought to 171 ° C by indirect heat exchange with the sodium silicate solution leaving the reactor at
    in the pipe.
    a solution at 192 ° C is obtained by
    188 seconds
    from 15.7 kg / h of water brought to 171 ° C using the aforementioned heat exchange.
    O
    five
    0 5
    0
    five
    The pure sodium silicate solution, obtained in the proportion of 46.9 kg / h, contains 42.6% by weight of sodium silicate, whose weight ratio was 2.
    Example 10. In the same installation, on the same principle and with the same quality of sand as in example 9, the proposed method is carried out by feeding to the reactor 25.5 kg / h of sand with an ambient temperature and 59.6 kg / an alkaline solution containing 21.4 wt.% or 12.7 kg / h, respectively, at a temperature of 213 s. The alkaline solution is passed at a flow rate of 3.25 m / h through a layer of sand that forms in the pipe.
    The resulting solution at 213 ° C is obtained by homogeneous and exothermic mixing of 34.27 kg / h of a concentrated aqueous solution of sodium hydroxide containing 37.2% by weight of NajO and brought to 192 by indirect heat exchange with sodium silicate solution from the reactor at 207 ° C from 25.23 kg / h of water brought to a temperature of 192 ° C by heat exchange of the same type as above.
    The pure sodium silicate solution, obtained in an amount of 85 kg / h, contains 45 wt.% Sodium silicate, in which the weight ratio was 2.
    Improving the efficiency of the process of obtaining solutions of alkali silicate using the coarse sand
    mole instead of finely divided silicon oxide (save energy for crushing and therefore, investment), eliminating mixing
    45 mixtures of sand - alkaline solution (saving investments and energy), eliminating: no specialization of 1x filtering devices (saving investments) and continuous operation without using additional energy from the outside.
    权利要求:
    Claims (2)
    [1]
    1. A method of obtaining a solution of alkali metal silicate with a mass ratio of silicon dioxide to alkali metal oxide not more than 2.5, including the interaction of a solution of hydroxide and alkali metal hydroxide
    5.13
    with quartz sand of a fraction of 0.13-0.85 mm at 160-225 ° C and a pressure higher than the saturated vapor pressure of the liquid phase of the system at a given temperature, so that, in order to simplify the process, the interaction is carried out by passing the solution with concentration of 11.2 - 26.7% (in terms of alkali metal oxide) at a speed of 3.25-10.8 m / h through a non-interleaved layer of quartz sand, both components being fed from top to bottom in a tubular vertical reactor with a silica silica mass ratio to an alkali metal oxide equal to (1, 015-2.51: 1.
    Editor Y. Sereda
    Compiled by G. Leontiev Tehred L. Serdyukova Proofreader M. Demchik
    Order 1905/57 Circulation 456 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, st. Project, 4
    16156
    [2]
    2. The method according to claim 1, 1 and 2 with the fact that the alkali metal hydroxide solution fed to the reactor is obtained by homogeneous and exothermic mixing of the concentrated alkali metal hydroxide solution and water, preheated by indirect heat exchange with a solution of silicate, an alkali metal leaving the reactor.
    ten
    Priority points:
    15.04.04 according to claim 1; 02/25/83 according to claim 2.
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    同族专利:
    公开号 | 公开日
    IT8367408D0|1983-04-14|
    BE896296A|1983-09-29|
    AU553156B2|1986-07-03|
    GB2119779B|1985-07-10|
    DE3313814C2|1986-07-03|
    CA1182276A|1985-02-12|
    GB2119779A|1983-11-23|
    AU1358783A|1983-10-20|
    FR2541667A2|1984-08-31|
    NL8301322A|1983-11-16|
    BR8301930A|1983-12-20|
    ES521540A0|1984-05-16|
    IT1160119B|1987-03-04|
    CH653977A5|1986-01-31|
    DE3313814A1|1983-10-27|
    ES8404960A1|1984-05-16|
    FR2541667B2|1986-07-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    BE649739A|
    FR1112807A|1953-09-05|1956-03-19|Hoechst Ag|Alkali silicates and process for their preparation|
    FR1382931A|1962-08-08|1964-12-24|Toyo Koatsu Ind Inc|Advanced process for the synthesis of urea|
    FR2462390B1|1979-07-25|1981-07-24|Ugine Kuhlmann|
    DE3002857A1|1980-01-26|1981-07-30|Henkel KGaA, 4000 Düsseldorf|METHOD FOR THE HYDROTHERMAL PRODUCTION OF SODIUM SILICATE SOLUTIONS|
    DE3002834A1|1980-01-26|1981-07-30|Henkel KGaA, 4000 Düsseldorf|METHOD FOR THE HYDROTHERMAL PRODUCTION OF SODIUM SILICATE SOLUTIONS IN A STATIC REACTION CONTAINER|GB8325477D0|1983-09-23|1983-10-26|Ici Plc|Alkali metal silicates|
    GB8325478D0|1983-09-23|1983-10-26|Ici Plc|Alkali metal silicates|
    GB8325479D0|1983-09-23|1983-10-26|Ici Plc|Alkali metal silicates|
    DE3423945A1|1984-06-29|1986-01-09|Henkel KGaA, 4000 Düsseldorf|METHOD AND DEVICE FOR THE CONTINUOUS HYDROTHERMAL PRODUCTION OF SODIUM SILICATE SOLUTIONS|
    DE3902751A1|1989-01-31|1990-08-02|Henkel Kgaa|METHOD FOR THE HYDROTHERMAL PRODUCTION OF SODIUM SILICATE SOLUTIONS WITH A HIGH SI02 : NA2MOLENE RATIO|
    DE3902753A1|1989-01-31|1990-08-02|Henkel Kgaa|METHOD FOR THE HYDROTHERMAL PRODUCTION OF POTASSIUM SILICATE SOLUTIONS WITH HIGH SI02 : K20-MOLE RATIO|
    CA2009035A1|1989-01-31|1990-07-31|Rudolf Novotny|Process for hydrothermal production of sodium silicate solutions|
    DE3902754A1|1989-01-31|1990-08-02|Henkel Kgaa|METHOD FOR THE HYDROTHERMAL PRODUCTION OF SODIUM SILICATE SOLUTIONS|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR8206563A|FR2525204B1|1982-04-16|1982-04-16|
    FR8303078A|FR2541667B2|1982-04-16|1983-02-25|PROCESS FOR PRODUCING ALKALI SILICATE SOLUTIONS IN A STATIC REACTOR|
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