WO2020140358A1 - 一种酸化剂载体用二氧化硅微球的制备方法 - Google Patents

一种酸化剂载体用二氧化硅微球的制备方法 Download PDF

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WO2020140358A1
WO2020140358A1 PCT/CN2019/085748 CN2019085748W WO2020140358A1 WO 2020140358 A1 WO2020140358 A1 WO 2020140358A1 CN 2019085748 W CN2019085748 W CN 2019085748W WO 2020140358 A1 WO2020140358 A1 WO 2020140358A1
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sulfuric acid
sodium silicate
silica microspheres
acidifier
reaction
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PCT/CN2019/085748
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English (en)
French (fr)
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胡金星
吴晓林
高海明
柴金鉴
李祥凯
孙玉军
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山东联科科技股份有限公司
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    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K20/00—Accessory food factors for animal feeding-stuffs
    • A23K20/20—Inorganic substances, e.g. oligoelements

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  • the invention relates to the field of preparation of silica, in particular to a preparation method of silica microspheres for acidifier carrier.
  • the feed additive acidifier is an important additive that follows antibiotics, along with probiotics, enzyme preparations, and micro-ecological preparations. It is an environmentally friendly additive that has no residue, no drug resistance, and no toxic effects. In recent years, acidulants and probiotics, enzyme preparations, flavoring agents, etc. have been listed as new green feed additives.
  • feed acidifiers in piglet feed, poultry feed, silage and other fields has become increasingly common and has significant effects.
  • there are still some problems such as the use of some acidifiers is unstable, the cost is high, the prepared premix is not easy to disperse, the absorption speed in the animal stomach is too fast, it is easy to absorb moisture and agglomerate, corrode the processing machinery, transportation equipment, etc.
  • the quality of the acidifier product is not only affected by the content of its active ingredients, but also has a very close relationship with the performance of its carrier.
  • the carrier generally uses silica.
  • the preparation methods of silica are mainly the precipitation method and the gas phase method. Since the raw materials used in the precipitation method are cheap and easily available, the production process and equipment are relatively simple, and the product price is low, so it is dominant.
  • the precipitation method mainly includes preparing a dilute solution with a certain concentration by using industrial water glass, and then adding an acid under certain conditions to precipitate the silica, and then preparing the silica after washing, filtering, drying and crushing.
  • silica carriers currently used in the acidifier industry are mostly in the form of fine powder, which has poor adsorption and fluidity, is easy to agglomerate, is not easy to disperse, and has a small amount of addition, which cannot meet the requirements of use and even bring quality. Accidents, therefore, a method for preparing silica is required, which is not only good in adsorption and fluidity, but also stable and not easy to agglomerate.
  • the present invention discloses a method for preparing silica microspheres for acidifier carrier, which specifically includes the following steps:
  • reaction liquid B Add sodium silicate to the synthesis kettle, pass steam under stirring to raise the temperature to 75-95°C, add water and stir to obtain reaction primer A, and add sulfuric acid to reaction primer A to acidify first. Until the solution pH is 7.5-11.5, reaction liquid B is obtained;
  • reaction solution C To the reaction solution B obtained in step (1), sulfuric acid and sodium silicate are simultaneously added for a synthesis reaction to obtain a reaction solution C;
  • step (3) Stop adding sodium silicate to the reaction solution C obtained in step (2), add only sulfuric acid for post-acidification, and check that the pH reaches 3.5-5.5. After curing, a thin slurry D is obtained;
  • step (3) After filtering and washing the thin slurry D obtained in step (3) to obtain a filter cake E, transfer the obtained filter cake E to a pulper, add a thickener, and obtain a slurry G;
  • step (4) After drying the slurry obtained in step (4), the silica microspheres for the acidifying agent carrier are obtained.
  • sodium silicate is a sodium silicate aqueous solution with a concentration of 20-30 Baume; the modulus of the sodium silicate is 2.80-3.30; the sulfuric acid is the mass fraction It is 30-60% sulfuric acid aqueous solution.
  • the amount of sodium silicate added is 15-25m 3 ; the concentration of sodium silicate in the reaction primer A is 13-15 Baume; the flow rate of the sulfuric acid is 5- 10m 3 /h, the addition time of the sulfuric acid is 40-60min, and the stirring speed is 22-57rpm.
  • step (2) flow rate of the sulfuric acid is 5-10m 3 / h, the flow rate of the sodium silicate is 15m 3 / h, the sulfuric acid and sodium silicate addition time is 15-30min.
  • the flow rate of the sulfuric acid is 50-70% of the flow rate of the sulfuric acid in the step (2), the feeding time of the sulfuric acid is 30-40 min; the curing time is 5-15 min.
  • the thickener in the step (4) is a polycarboxylic acid thickener; preferably, the polycarboxylic acid thickener is sodium polyacrylate.
  • the drainage conductivity during the washing process is 5.0-10.0 ms/cm.
  • the drying method is to perform the first stage drying after pressure spray drying, and then enter the boiling bed to perform the second stage drying; the temperature of the first stage drying is 350-550°C, The drying pressure in the first stage is -50 to -250 Pa; the drying temperature in the second stage is 150 to 250° C., and the drying pressure in the second stage is -350 to -150 Pa;
  • the temperature of the reaction in the reaction steps (1)-(3) in the present invention is maintained at 75-95°C.
  • the present invention provides a production technology of silica microspheres, the product has a coarse appearance, and has a certain strength, the particle size of the microspheres is uniform, and it does not break or agglomerate during the adsorption of the acidulant, and the adsorption speed Fast, good fluidity and adsorption, can improve the quality level of acidulant and production efficiency, and reduce the manufacturing cost of feed acidifier.
  • the prepared silica microspheres for acidifier carrier have high adsorption.
  • the invention adopts a polycarboxylic acid thickener to help increase the viscosity of the material before drying, thereby improving the surface hardness of the product after drying and the particle strength of the silica microspheres.
  • the present invention adopts pressure spray drying combined with a fluidized bed drying method.
  • Fluidized bed drying uses indirect heated clean air to ensure the particle size, strength and fluidity of the product, which is conducive to the formation of acidifiers and improves acidifiers. Stability.
  • Example 1 A method for preparing silica microspheres for acidifier carrier
  • reaction liquid B Add sodium silicate to the synthesis kettle, pass steam under stirring to raise the temperature to 75°C, add water and stir to obtain reaction bottom material A, add sulfuric acid to the reaction bottom material A to acidify first, until the solution When the pH is 8.0, reaction liquid B is obtained;
  • step (2) To the reaction solution B obtained in step (1), sulfuric acid and sodium silicate are simultaneously added for a synthesis reaction, and the reaction solution C is obtained;
  • step (3) Stop adding sodium silicate to the reaction solution C obtained in step (2), add only sulfuric acid for post-acidification, detect the pH reaches 4.5, and obtain a thin slurry D after aging;
  • step (3) After filtering and washing the thin slurry D obtained in step (3) to obtain a filter cake E, transfer the obtained filter cake E to a pulper, add a thickener, and obtain a slurry G;
  • step (4) After drying the slurry obtained in step (4), the silica microspheres for the acidifying agent carrier are obtained.
  • the concentration of sodium silicate is 20; the modulus of the sodium silicate is 2.80; and the sulfuric acid is a sulfuric acid aqueous solution with a mass fraction of 60%.
  • the amount of sodium silicate added is 15m 3 ; the concentration of sodium silicate in the reaction primer A is 14.3 Baume; the flow rate of the sulfuric acid is 5m 3 /h, so The addition time of the sulfuric acid is 45 min, and the stirring speed is 35 rpm.
  • the flow rate of the sulfuric acid is 5 m 3 /h
  • the flow rate of the sodium silicate is 15 m 3 /h
  • the feeding time of the sulfuric acid and sodium silicate is 20 min.
  • the flow rate of the sulfuric acid is the flow rate of the sulfuric acid in the step (2) is 2.5 m 3 /h, the feeding time of the sulfuric acid is 30 min; the curing time is 10 min.
  • the thickener in the step (4) is sodium polyacrylate, the addition amount of the sodium polyacrylate is 5.0 kg, and the pH of the slurry G is 6.3.
  • the drainage conductivity during the washing process is 5.0 ms/cm.
  • the drying method is to perform the first stage drying after pressure spray drying, and then enter the boiling bed to perform the second stage drying; the temperature of the first stage drying is 450°C, the first The drying pressure in one stage is -50 Pa; the drying temperature in the second stage is 160° C., and the drying pressure in the second stage is -200 Pa.
  • the temperature of the reaction in the reaction steps (1)-(3) was kept at 75°C.
  • Embodiment 2 A method for preparing silica microspheres for acidifier carrier
  • step (2) To the reaction solution B obtained in step (1), sulfuric acid and sodium silicate are simultaneously added for a synthesis reaction, and the reaction solution C is obtained;
  • step (3) Stop adding sodium silicate to the reaction solution C obtained in step (2), add only sulfuric acid for post-acidification, detect the pH reaches 4.5, and obtain a thin slurry D after aging;
  • step (3) After filtering and washing the thin slurry D obtained in step (3) to obtain a filter cake E, transfer the obtained filter cake E to a pulper, add a thickener, and obtain a slurry G;
  • step (4) After drying the slurry obtained in step (4), the silica microspheres for the acidifying agent carrier are obtained.
  • sodium silicate is an aqueous solution of sodium silicate with a concentration of 30 Baume; the modulus of the sodium silicate is 3.30; and the sulfuric acid is a mass fraction of 30% Sulfuric acid aqueous solution.
  • the amount of sodium silicate added is 25m 3 ; the concentration of sodium silicate in the reaction primer A is 10.5 Baume; the flow rate of the sulfuric acid is 10m 3 /h, so The addition time of the sulfuric acid was 60 min, and the stirring speed was 22 rpm.
  • the flow rate of the sulfuric acid is 10 m 3 /h
  • the flow rate of the sodium silicate is 15 m 3 /h
  • the feeding time of the sulfuric acid and sodium silicate is 30 min.
  • the flow rate of the sulfuric acid is 5 m 3 /h, the feeding time of the sulfuric acid is 30 min; the curing time is 15 min.
  • the thickener in the step (4) is sodium polyacrylate, the addition amount of the sodium polyacrylate is 10.0 kg, and the pH of the slurry G is 6.9.
  • the drainage conductivity during the washing process is 8.0 ms/cm.
  • the drying process in the step (5) is after pressure spray drying, followed by the first stage drying, and then enters the ebullating bed to perform the second stage drying.
  • the effervescent bed drying uses clean air heated indirectly by steam; the first stage drying The temperature is 550 °C, the first stage drying pressure is -150Pa; the second stage drying temperature is 210 °C, the second stage drying pressure is -200Pa in the reaction steps (1)-(3) The temperature of the reaction was kept at 95°C.
  • Embodiment 3 A method for preparing silica microspheres for acidifier carrier
  • step (2) To the reaction solution B obtained in step (1), sulfuric acid and sodium silicate are simultaneously added for a synthesis reaction, and the reaction solution C is obtained;
  • step (3) Stop adding sodium silicate to the reaction solution C obtained in step (2), add only sulfuric acid for post-acidification, detect pH reaches 4.5, and obtain a thin slurry after curing to obtain a thin slurry D;
  • step (3) After filtering and washing the thin slurry D obtained in step (3) to obtain a filter cake E, transfer the obtained filter cake E to a pulper, add a thickener, and obtain a slurry G;
  • step (4) After drying the slurry obtained in step (4), the silica microspheres for the acidifying agent carrier are obtained.
  • sodium silicate is an aqueous solution of sodium silicate with a concentration of 20 Baume; the modulus of the sodium silicate is 3.30; the sulfuric acid is a mass fraction of 60% Sulfuric acid aqueous solution.
  • the amount of sodium silicate added is 25m 3 ; the concentration of sodium silicate in the reaction primer A is 12 Baume; the flow rate of the sulfuric acid is 6.0m 3 /h, The addition time of the sulfuric acid was 50 min, and the stirring speed was 22 rpm.
  • the flow rate of the sulfuric acid is 8 m 3 /h
  • the flow rate of the sodium silicate is 15.0 m 3 /h
  • the feeding time of the sulfuric acid and sodium silicate is 20 min.
  • the flow rate of the sulfuric acid is 5.0 m 3 /h, the feeding time of the sulfuric acid is 30 min; the curing time is 15 min.
  • the thickener in the step (4) is sodium polyacrylate, the addition amount of the sodium polyacrylate is 10.0 Kg, and the pH of the slurry G is 6.6.
  • the drainage conductivity during the washing process is 8.0 ms/cm.
  • the drying process in the step (5) is after pressure spray drying, followed by the first stage drying, and then enters the ebullating bed to perform the second stage drying.
  • the effervescent bed drying uses clean air heated indirectly by steam; the first stage drying The temperature is 550 °C, the first stage drying pressure is -150Pa; the second stage drying temperature is 210 °C, the second stage drying pressure is -200Pa, the boiling heat source of the boiling bed is steam exchange Clean air heated by the heater.
  • the reaction temperature in the reaction steps (1)-(3) is kept at 85°C
  • the preparation method is basically the same as Example 1, and the difference from Example 1 is that the modulus of the sodium silicate is 3.55.
  • Comparative Example 2 A method for preparing silica microspheres for acidifier carrier
  • the preparation method is basically the same as Example 1, and the difference from Example 1 is that the thickener is sodium bicarbonate.
  • silica microspheres for acidifier carrier provided in Examples 1-3 of the present invention have good thermal stability, high hardness, and low particle crushing rate, and can be effective for fumaric acid Adsorption.

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Abstract

一种酸化剂载体用二氧化硅微球的制备方法，包括以下步骤：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温，加入水搅拌得到反应底料A，向反应底料A中加入硫酸，先酸化至一定pH，向得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，得到反应液C；然后停止加入硅酸钠，只加入硫酸进行后酸化至一定pH，熟化后得到稀浆料D；稀浆料D经过滤、洗涤、制浆、增稠，干燥后，即得到所述的酸化剂载体用二氧化硅微球。由此制备的二氧化硅微球，微球的粒径均一，不易破碎，不结团，吸附速度快，流散性和吸附性好。

Description

一种酸化剂载体用二氧化硅微球的制备方法 技术领域
本发明涉及领域二氧化硅的制备领域，特别涉及一种酸化剂载体用二氧化硅微球的制备方法。
背景技术
饲料添加剂酸化剂是继抗生素之后，与益生素、酶制剂、微生态制剂等并列的重要添加剂，是一种无残留、无抗药性、无毒害作用的环保型添加剂。近年来，酸化剂与益生素、酶制剂、香味剂等并列为新型的绿色饲料添加剂，饲料酸化剂在仔猪饲料、家禽饲料、青贮饲料等领域的应用也日益普遍且效果显著。但仍存在一些问题，如有些酸化剂使用效果不稳定，成本高，制成预混料不易分散，在动物胃中吸收速度过快，易吸湿结块，腐蚀加工机械、运输设备等。酸化剂产品质量的优劣，不仅受其活性成分含量影响，还与其载体性能有非常密切的关系。载体一般使用二氧化硅，目前，二氧化硅的制备方法主要是沉淀法和气相法，由于沉淀法所用原料便宜易得，生产工艺和设备较为简单，产品售价低，因此占主导地位。沉淀法主要包括是采用工业水玻璃配制成一定浓度的稀溶液，然后在一定条件下加入某种酸，使二氧化硅沉淀出来，再经清洗、过滤、干燥、粉碎后制备得到二氧化硅。然而，目前酸化剂行业使用的二氧化硅载体外观多为细粉状，其吸附性和流动性差，易结块，不易分散，添加量偏小，不能较好地满足使用要求，甚至带来质量事故，因此需要一种二氧化硅的制备方法，其不仅吸附性和流动性好，而且稳定不易结团。
发明内容
为解决上述技术问题，本发明公开了一种酸化剂载体用二氧化硅微球的制备方法，具体包括以下步骤：
(1)：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温至75-95℃，加入水搅拌得到反应底料A，向反应底料A中加入硫酸进行先酸化，至溶液pH为7.5-11.5，得到反应液B；
(2)：向步骤(1)得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，得到反应液C；
(3)：步骤(2)得到的反应液C中停止加入硅酸钠，只加入硫酸进行后酸化，检测pH达到3.5-5.5，熟化后得到稀浆料D；
(4)：将步骤(3)得到的稀浆料D经过滤、洗涤后得到滤饼E，将得到的滤饼E转移至制浆机，加入增稠剂，得到浆料G；
(5)：将步骤(4)得到的浆料干燥后，即得到所述的酸化剂载体用二氧化硅微球。
所述的步骤(1)-(3)中：硅酸钠为浓度为20-30波美度的硅酸钠水溶液；所述硅酸钠的模数为2.80-3.30；所述硫酸为质量分数为30-60％的硫酸水溶液。
所述步骤(1)中：所述硅酸钠的加入量为15-25m 3；所述反应底料A中硅酸钠的浓度为13-15波美度；所述硫酸的流速为5-10m 3/h，所述硫酸的加入时间为40-60min，所述搅拌速度为22-57rpm。
所述步骤(2)中：所述硫酸的流速为5-10m 3/h，所述硅酸钠的流速为15m 3/h，所述硫酸和硅酸钠的加料时间为15-30min。
所述步骤(3)中：所述硫酸的流速为所述步骤(2)中硫酸流速的50-70％，所述硫酸的加料时间为30-40min；所述熟化时间为5-15min。
所述步骤(4)中的增稠剂为聚羧酸增稠剂；优选地，所述的聚羧酸增稠剂为聚丙烯酸钠。
所述步骤(4)中：所述洗涤过程中的排水电导率为5.0-10.0ms/cm。
所述步骤(5)中：所述干燥方法为在压力喷雾干燥后进行第一段干燥后，然后进入沸腾床进行第二段干燥；所述第一段干燥的温度为350-550℃， 所述第一段干燥压力为-50～-250Pa；所述第二段干燥的温度为150-250℃，所述第二段干燥压力为-350～-150Pa；
无特别说明：本发明中的反应步骤(1)-(3)中的反应的温度均保持在75-95℃。
本发明的有益效果是：
(1)本发明提供了一种二氧化硅微球生产技术，产品外观粗大化，并且具有一定强度，微球的粒径均一，并且在吸附酸化剂过程中不破碎，不结团，吸附速度快，流散性和吸附性好，可以提高酸化剂质量水平和生产效率，降低了饲料酸化剂的制造成本。
(2)本发明通过调整硅酸钠中硅酸钠的模数、各个步骤中硅酸钠和硫酸的浓度及加入时间，制备出的酸化剂载体用二氧化硅微球具有高吸附性。
(3)本发明通过选用聚羧酸增稠剂，有利于增加干燥前的物料粘度，从而提高干燥后产品表面硬度和二氧化硅微球的颗粒强度。
(4)本发明通过采用压力喷雾干燥结合沸腾床的干燥方式，沸腾床干燥选用蒸汽间接加热的洁净空气，保证了产品的粒度、强度和流散性，有利于酸化剂的赋型、提高酸化剂的稳定性。
具体实施方式
下面将对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。
实施例1一种酸化剂载体用二氧化硅微球的制备方法
包括以下步骤：
(1)：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温至75℃，加入水搅拌得到反应底料A，向反应底料A中加入硫酸进行先酸化，至溶液pH为8.0，得到反应液B；
(2)：向步骤(1)得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，反应得到反应液C；
(3)：步骤(2)得到的反应液C中停止加入硅酸钠，只加入硫酸进行后酸化，检测pH达到4.5，熟化后得到稀浆料D；
(4)：将步骤(3)得到的稀浆料D经过滤、洗涤后得到滤饼E，将得到的滤饼E转移至制浆机，加入增稠剂，得到浆料G；
(5)：将步骤(4)得到的浆料干燥后，即得到所述的酸化剂载体用二氧化硅微球。
所述的步骤(1)-(3)中：硅酸钠为浓度为20；所述硅酸钠的模数为2.80；所述硫酸为质量分数为60％的硫酸水溶液。
所述步骤(1)中：所述硅酸钠的加入量为15m 3；所述反应底料A中硅酸钠的浓度为14.3波美度；所述硫酸的流速为5m 3/h，所述硫酸的加入时间为45min，所述搅拌速度为35rpm。
所述步骤(2)中：所述硫酸的流速为5m 3/h，所述硅酸钠的流速为15m 3/h，所述硫酸和硅酸钠的加料时间为20min。
所述步骤(3)中：所述硫酸的流速为所述步骤(2)中硫酸流速为2.5m 3/h，所述硫酸的加料时间为30min；所述熟化时间为10min。
所述步骤(4)中的增稠剂为聚丙烯酸钠，所述聚丙烯酸钠的加入量为5.0kg，所述浆料G的pH为6.3。
所述步骤(4)中：所述洗涤过程中的排水电导率为5.0ms/cm。
所述步骤(5)中：所述干燥方法为在压力喷雾干燥后进行第一段干燥后，然后进入沸腾床进行第二段干燥；所述第一段干燥的温度为450℃，所述第一段干燥压力为-50Pa；所述第二段干燥的温度为160℃，所述第二段干燥压力为-200Pa。
反应步骤(1)-(3)中的反应的温度均保持在75℃。
实施例2一种酸化剂载体用二氧化硅微球的制备方法
包括以下步骤：
(1)：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温至95℃，加入水搅拌得到反应底料A，向反应底料A中加入硫酸进行先酸化，至溶液pH为10.0，得到反应液B；
(2)：向步骤(1)得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，反应得到反应液C；
(3)：步骤(2)得到的反应液C中停止加入硅酸钠，只加入硫酸进行后酸化，检测pH达到4.5，熟化后得到稀浆料D；
(4)：将步骤(3)得到的稀浆料D经过滤、洗涤后得到滤饼E，将得到的滤饼E转移至制浆机，加入增稠剂，得到浆料G；
(5)：将步骤(4)得到的浆料干燥后，即得到所述的酸化剂载体用二氧化硅微球。
所述的步骤(1)-(3)中：硅酸钠为浓度为30波美度的硅酸钠水溶液；所述硅酸钠的模数为3.30；所述硫酸为质量分数为30％的硫酸水溶液。
所述步骤(1)中：所述硅酸钠的加入量为25m 3；所述反应底料A中硅酸钠的浓度为10.5波美度；所述硫酸的流速为10m 3/h，所述硫酸的加入时间为60min，所述搅拌速度为22rpm。
所述步骤(2)中：所述硫酸的流速为10m 3/h，所述硅酸钠的流速为15m 3/h，所述硫酸和硅酸钠的加料时间为30min。
所述步骤(3)中：所述硫酸的流速为5m 3/h，所述硫酸的加料时间为30min；所述熟化时间为15min。
所述步骤(4)中的增稠剂为聚丙烯酸钠，所述聚丙烯酸钠的加入量为10.0kg，所述浆料G的pH为6.9。
所述步骤(4)中：所述洗涤过程中的排水电导率为8.0ms/cm。
所述步骤(5)中的干燥过程为在压力喷雾干燥后进行第一段干燥后，然后进入沸腾床进行第二段干燥，沸腾床干燥选用蒸汽间接加热的洁净空气；所述第一段干燥的温度为550℃，所述第一段干燥压力为-150Pa；所述 第二段干燥的温度为210℃，所述第二段干燥压力为-200Pa反应步骤(1)-(3)中的反应的温度均保持在95℃。
实施例3一种酸化剂载体用二氧化硅微球的制备方法
包括以下步骤：
(1)：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温至85℃，加入水搅拌得到反应底料A，向反应底料A中加入硫酸进行先酸化，至溶液pH为9.5，得到反应液B；
(2)：向步骤(1)得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，反应得到反应液C；
(3)：步骤(2)得到的反应液C中停止加入硅酸钠，只加入硫酸进行后酸化，检测pH达到4.5，熟化后得到稀浆料得到稀浆料D；
(4)：将步骤(3)得到的稀浆料D经过滤、洗涤后得到滤饼E，将得到的滤饼E转移至制浆机，加入增稠剂，得到浆料G；
(5)：将步骤(4)得到的浆料干燥后，即得到所述的酸化剂载体用二氧化硅微球。
所述的步骤(1)-(3)中：硅酸钠为浓度为20波美度的硅酸钠水溶液；所述硅酸钠的模数为3.30；所述硫酸为质量分数为60％的硫酸水溶液。
所述步骤(1)中：所述硅酸钠的加入量为25m 3；所述反应底料A中硅酸钠的浓度为12波美度；所述硫酸的流速为6.0m 3/h，所述硫酸的加入时间为50min，所述搅拌速度为22rpm。
所述步骤(2)中：所述硫酸的流速为8m 3/h，所述硅酸钠的流速为15.0m 3/h，所述硫酸和硅酸钠的加料时间为20min。
所述步骤(3)中：所述硫酸的流速为5.0m 3/h，所述硫酸的加料时间为30min；所述熟化时间为15min。
所述步骤(4)中的增稠剂为聚丙烯酸钠，所述聚丙烯酸纳的加入量为10.0Kg，所述浆料G的pH为6.6。
所述步骤(4)中：所述洗涤过程中的排水电导率为8.0ms/cm。
所述步骤(5)中的干燥过程为在压力喷雾干燥后进行第一段干燥后，然后进入沸腾床进行第二段干燥，沸腾床干燥选用蒸汽间接加热的洁净空气；所述第一段干燥的温度为550℃，所述第一段干燥压力为-150Pa；所述第二段干燥的温度为210℃，所述第二段干燥压力为-200Pa，所述沸腾床的干燥热源为蒸汽换热器加热的洁净空气。
反应步骤(1)-(3)中的反应的温度均保持在85℃
对比例1一种酸化剂载体用二氧化硅微球的制备方法
其制备方法基本同实施例1，与实施例1的差别在于：所述的硅酸钠的模数为3.55。
对比例2一种酸化剂载体用二氧化硅微球的制备方法
其制备方法基本同实施例1，与实施例1的差别在于：所述的增稠剂为碳酸氢钠。
将上述实施例1-3及对比例1-2中的制备方法制备得到的酸化剂载体用二氧化硅微球进行性能测试，测试结果如下表所示：
表1
Figure PCTCN2019085748-appb-000001
从表1数据可以看出，本发明实施例1-3提供的酸化剂载体二氧化硅为微球的DBP吸收量为2.55-2.80ml/g，其吸收量高于对比例1。
表2
Figure PCTCN2019085748-appb-000002
从表2中的数据可以看出，本发实施例1-3提供的酸化剂载体用二氧化硅微球的热稳定性好，硬度高，颗粒破碎率低，并且可以对富马酸进行有效吸附。
表3
Figure PCTCN2019085748-appb-000003
从表3中的数据可以看出，本发明实施例1-3提供的酸化剂载体二氧化硅微球具有较高的比表面积，并且分散性好，不团聚。
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。另外，各个实施例之间的技术方案可以相互结合，但是必须是以本领域普通技术人员能够实现为基础，当技术方案的结合出现相互矛盾或无法实现时应当认为这种技术方案的结合不存在，也不在本发明要求的保护范围之内。

Claims (9)

  1. 一种酸化剂载体用二氧化硅微球的制备方法，其特征在于，包括以下步骤：
    (1)：将硅酸钠加入到合成釜中，在搅拌的条件下通入蒸汽升温至75-95℃，加入水搅拌得到反应底料A，向反应底料A中加入硫酸进行先酸化，至溶液pH为7.5-11.5，得到反应液B；
    (2)：向步骤(1)得到的反应液B中同时加入硫酸和硅酸钠进行合成反应，得到反应液C；
    (3)：步骤(2)得到的反应液C中停止加入硅酸钠，只加入硫酸进行后酸化，检测pH达到3.5-5.5，熟化后得到稀浆料D；
    (4)：将步骤(3)得到的稀浆料D经过滤、洗涤后得到滤饼E，将得到的滤饼E转移至制浆机，加入增稠剂，得到浆料G；
    (5)：将步骤(4)得到的浆料干燥后，即得到所述的酸化剂载体用二氧化硅微球。
  2. 如权利要求1所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述的步骤(1)-(3)中：硅酸钠为浓度为20-30波美度的硅酸钠水溶液；所述硅酸钠的模数为2.80-3.30；所述硫酸为质量分数为30-60％的硫酸水溶液。
  3. 如权利要求2所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述步骤(1)中：所述硅酸钠的加入量为15-25m 3；所述反应底料A中硅酸钠的浓度为13-15波美度；所述硫酸的流速为5-10m 3/h，所述硫酸的加入时间为40-60min，所述搅拌速度为22-57rpm。
  4. 如权利要求2所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述步骤(2)中：所述硫酸的流速为5-10m 3/h，所述硅酸钠的流速为15m 3/h，所述硫酸和硅酸钠的加料时间为15-30min。
  5. 如权利要求2所述的酸化剂载体用二氧化硅微球的制备方法，其特征碍于，所述步骤(3)中：所述硫酸的流速为所述步骤(2)中硫酸流速的50-70％，所述硫酸的加料时间为30-40min；所述熟化时间为5-15min。
  6. 如权利要求1所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述步骤(4)中的增稠剂为聚羧酸增稠剂。
  7. 如权利要求1所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述步骤(4)中：所述洗涤过程中的排水电导率为5.0-10.0ms/cm。
  8. 如权利要求1所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述步骤(5)中：所述干燥方法为用压力喷雾干燥方式进行第一段干燥，然后进入沸腾床进行第二段干燥。
  9. 如权利要求8所述的酸化剂载体用二氧化硅微球的制备方法，其特征在于，所述第一段干燥的温度为350-550℃，所述第一段干燥压力为-250～-50Pa；所述第二段干燥的温度为150-250℃，所述第二段干燥压力为-350～-150Pa。
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